Process for manufacture of 2-chloro-1,1,1-trifluoropropene

ABSTRACT

The present invention pertains to a novel process of manufacturing the compound 2,3,3,3-tetrafluoropropene (1234yf). The compound 1234yf is the newest refrigerant with zero OPD (Ozone Depleting Potential) and zero GWP (Global Warming Potential). Thus, the invention relates to a process, involving a carbene generation route, for the manufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf), of the compound 243db (2,3-dichloro-1,1,1-trifluoropropane), and optionally of the compound 2-chloro-1,1,1-trifluoropropene (1233xf) via carbene route and compound 243db (2,3-dichloro-1,1,1-trifluoropropane). The invention also relates to a process for the manufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf), wherein the compound 243db (2,3-dichloro-1,1,1-trifluoropropane) serves as a starting material, for the manufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf). Further, the invention relates to a process for the manufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf), and of the compound 243db (2,3-dichloro-1,1,1-trifluoropropane), the initial starting materials are selected from the group consisting of com-pound 123 (2,2-dichloro-1,1,1-trifluoroethane), compound 124 (2-chloro-1,1,1,2-tetrafluoroethane), and compound 125 (pentafluoroethane).

BACKGROUND OF THE INVENTION Field of the Disclosure

The invention relates to a process for the manufacture of the compound2,3-dichloro-1,1,1-trifluoropropane (243db). The invention also relatesto a process for the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf), wherein the compound2,3-dichloro-1,1,1-trifluoropropane (243db) serves as a startingmaterial. Further, the invention relates to a process for themanufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf), of thecompound 2,3-dichloro-1,1,1-trifluoropropane (243db), and optionally ofthe compound 2-chloro-1,1,1-trifluoropropene (1233xf), wherein theinitial starting materials are selected from compound 123(2,2-dichloro-1,1,1-trifluoroethane), from compound 124(2-chloro-1,1,1,2-tetrafluoroethane), or from compound 125(pentafluoroethane).

Description of Related Art

The compound 1234yf is the fourth generation refrigerant showing no ODP(Ozone Depleting Potential), and showing a GWP (Global WarmingPotential) of less than 1. In comparison the former refrigerantcandidate has shown a GWP of 1500.

The only drawback of this fourth generation refrigerant in view of itsapplication is the flammability, like described in a report ofBundesanstaltfür Materialforschung (“Federal Institute of MaterialScience”, Germany):(web.archive.org/web/20120816103321/http://www.umweltbundesamt.de/produkte/dokumente/test_report_hfo1234yf_2010_06.pdf).

The synthesis routes for the compound 2,3,3,3-tetrafluoropropene(1234yf) known in the state of the art performed in liquid phase and gasphase are either giving mixtures, have low conversion rates (energyconsuming recycling streams in industrial plant) or are just notpracticable in industrial scale due to pure safety and availability ofstarting materials.

Most common synthesis routes for the compound 2,3,3,3-tetrafluoropropene(1234yf) are the one from Honeywell like described in WO2009/018561according to Scheme A.

Alone the synthesis of the starting material tetrachloropropene is afour step synthesis out of 1,2,3-trichloropropane (see, e.g.,US2007/0197842), which is already a downstream product of allylchloride;see Scheme B.

Other routes described in the state of the art, e.g., by Honeywell, areon the same level of complexity like described in WO2008/002499 thesynthesis out of 245eb, of 1234yf and the isomers 1234ze (on the marketas “Solstice”); see Scheme C.

The compound HFC 245eb can be prepared by the hydrogenation ofCF₃CCIFCCI₂F (CFC-215bb) over a palladium on carbon catalyst asdisclosed in WO 2008/002501 A2, and which is incorporated herein byreference in its entirety, or by the hydrogenation of CF₃CF═CFH asdisclosed by Du Pont in WO 2008/002499; see Scheme D.

In US 2005/0245773 Honeywell is disclosing a three-step process toproduce 1,1,1,3-tetrafluororopene (1234ze isomeric mixture) but this1234 isomer seems to have some lower market importance; see Scheme E.

Furthermore, Archema describes the synthesis of2,3,3,3-tetrafluoropropene (1234yf) in WO2013/114015 (corresponding toUS2015/0080619) out of chlorinated propanes like pentachloropropanes ingas phase over chromium catalyst; as shown for example in Scheme F.

In an alternative synthesis route of Archema, the synthesis starts fromHFP, and is described, for example, in WO 2010/029240, WO 2009/118632,US 2012/0136183, U.S. Pat. No. 8,841,493, and in U.S. Pat. No.9,018,429; as shown for example in Scheme G.

Furthermore, the synthesis of 243db, and of 1233xf out of 243db, isknown from WO 2017/013406, but 243db is prepared out of expensivetrifluoropropene.

In general the generation of dihalogenatedcarbenes, e.g., out of CF₂ClH(HCFC 22) for production of tetrafluoroethylene (TFE) is well known andpracticed in very large industrial scale. Also the generation ofdifluorocarbene out of halogenodifluoro acetates is known, but lessrelevant for production of high volume materials like refrigerants. TFEimprovements are described by Dae Jin Sung, Dong Ju Moon, Yong Jun Lee,Suk-In Hong: Catalytic Pyrolysis of Difluorochloromethane to ProduceTetrafluoroethylene. In: International Journal of Chemical ReactorEngineering. 2, 2004, doi:10.2202/1542-6580.1065 and in CN 101973842, CN102516024 and CN 102491872. First applications also linked to TFE weredisclosed, e.g., in 1962 by Farbwerke Hoechst in DE 1217946, wherecompound HCFC 22 is pyrolyzed in presence of overheated water vapor,Asahi Glass U.S. Pat. No. 3,459,818, and also combined production of TFEand HFP as in ICI's patent EP 0287219.

An improved industrially feasible process is described by DuPont in WO02/06193 using gold lined equipment and improved parameters whichreduces undesired by-product formation and enhances productivity, e.g.,necessitating less cleaning from polymerized side product materials.U.S. Pat. No. 2,551,571 also filed by Du Pont discloses already similareffects by using a silver tube. Recent investigations made by UniversityBayreuth describe the preparation of different fluoroolefins in SiCmicroreactors (www.dbu.de/OPAC/ab/DBU-Abschlussbericht-AZ-31819.pdf).These newest results were presented in a Poster on Dechema“JahrestreffenReaktionstechnik” 2018 in Würzburg and des “22ndInternational Symposium on Fluorine” in Oxford.

OBJECTS OF THE INVENTION

It is an object of the present invention to provide a high efficientprocess for the manufacture of the compound 2,3,3,3-tetrafluoropropene(1234yf), of the compound 2,3-dichloro-1,1,1-trifluoropropane (243db),and optionally of the compound 2-chloro-1,1,1-trifluoropropene (1233xf).

It is preferably an object of the present invention to provide a highefficient process for the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf), and wherein the compound of thecompound 2,3-dichloro-1,1,1-trifluoropropane (243db) serves as astarting material in the process for the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf).

It is another object of the present invention to provide a highefficient process for the manufacture of the compound 243db(2,3-dichloro-1,1,1-trifluoropropane).

It is preferably still another object of the present invention toprovide a high efficient process for the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf), and wherein the compound 243db(2,3-dichloro-1,1,1-trifluoropropane) serves as a starting material inthe process for the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf).

It is still another object of the present invention to provide a highefficient process for the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf), and wherein the initial startingmaterial is a compound selected from the group consisting of compound123 (2,2-dichloro-1,1,1-trifluoroethane), compound 124(2-chloro-1,1,1,2-tetrafluoroethane), and compound 125(pentafluoroethane), and can serve as a starting material in the processfor the manufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf).Herein, preferably it is an object of the present invention that thecompound 123 (2,2-dichloro-1,1,1-trifluoroethane can serve as theinitial starting material in the process for the manufacture of thecompound 2,3,3,3-tetrafluoropropene (1234yf).

SUMMARY OF THE INVENTION

The objects of the invention are solved as defined in the claims, anddescribed herein after in detail. In particular, the present inventionpertains to a novel process, in particular, of manufacturing thecompound 2,3,3,3-tetrafluoropropene (1234yf), and of the compound2,3-dichloro-1,1,1-trifluoropropane (243db). The compound 1234yf is thenewest refrigerant with zero OPD (Ozone Depleting Potential) and zeroGWP (Global Warming Potential). Herein, the processes of the presentinvention have in common that the manufacture of the compounds involveat least one carbene generation step.

In chemistry, a carbene is a molecule containing a neutral carbon atomwith a valence of two and two unshared valence electrons. The generalformula is R—C(:)—R′ or R═C(:) where the R and R′ represent organiccarbon substituents or hydrogen atoms, and (:) represents two unsharedvalence electrons of the carbon atom (C).

In the context of the present invention, a carbene of interest in theprocesses of manufacturing compounds according to the objects of theinvention, is generated out of a trifluoroethane compound of the formulaCF₃—CHX_(n)Y_(2-n), wherein X and Y, each independently denotes ahalogen atom selected from the group consisting of fluorine (F) andchlorine (Cl); n is an integer of 1 or 2.

The preferred a halogen atom of the group of fluorine (F) and chlorine(Cl) is chlorine (Cl), for example, trifluoromethyl chloride.

The preferred starting compounds for generating a carbene of interest inthe processes of manufacturing compounds according to the objects of theinvention, having a formula CF₃—C(:)X, is a trifluoroethane compound ofthe formula CF₃—CHX_(n)Y_(2-m), selected from the group consisting ofcompound 123 (2,2-dichloro-1,1,1-trifluoroethane), compound 124(2-chloro-1,1,1,2-tetrafluoroethane), and compound 125(pentafluoroethane).

The said carbene of interest in the processes of manufacturing compoundsaccording to the objects of the invention, having the said formulaCF₃—C(:)X, is reacted with a methyl halogenide compound of formula CH₃X,wherein X denotes a halogen atom selected from the group consisting offluorine (F), chlorine (Cl), bromine (Br), and iodine (J). The preferreda halogen atom is, however, selected from the group consisting offluorine (F) and chlorine (Cl).

Although, a methyl halogenide compound of the formula CH₃X, wherein Xdenotes a halogen atom from the group of bromine (Br) and iodine (J),may be employed, for example, methyl bromide (CH₃Br) or methyl iodide(CH₃₁), this variant of the invention presently is economically lessfeasible, than variant of the invention variant of the inventionemploying a methyl halogenide compound of the formula CH₃X, wherein Xdenotes a halogen atom from the preferred group of fluorine (F) andchlorine (Cl), for example, preferably methyl chloride (CH₃C1).

In this context of manufacturing compounds by a process involving atleast one carbene generation step, the present invention pertains to anovel process, in particular, of manufacturing the compound2,3,3,3-tetrafluoropropene (1234yf), and of the compound2,3-dichloro-1,1,1-trifluoropropane (243db). The invention also relatesto a process for the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf), wherein the compound 243db(2,3-dichloro-1,1,1-trifluoropropane) serves as a starting material, forthe manufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf).

Further, the invention relates to a process for the manufacture of thecompound 2,3,3,3-tetrafluoropropene (1234yf), of the compound2,3-dichloro-1,1,1-trifluoropropane (243db), and optionally of thecompound 2-chloro-1,1,1-trifluoropropene (1233xf), wherein the initialstarting materials are selected from compound 123(2,2-dichloro-1,1,1-trifluoroethane), from compound 124(2-chloro-1,1,1,2-tetrafluoroethane), or from compound 125(pentafluoroethane).

Further, the invention relates to a process for the manufacture of thecompound 2,3,3,3-tetrafluoropropene (1234yf), of the compound2,3-dichloro-1,1,1-trifluoropropane (243db), and optionally of thecompound 2-chloro-1,1,1-trifluoropropene (1233xf), wherein the initialstarting materials are selected from the group consisting of compound123 (2,2-dichloro-1,1,1-trifluoroethane), compound 124(2-chloro-1,1,1,2-tetrafluoroethane), and compound 125(pentafluoroethane). The compound 123(2,2-dichloro-1,1,1-trifluoroethane is preferred as the initial startingmaterial. In particular, the process of the invention involves a carbenegeneration step, and wherein the carbene formed is further reactedtowards the said targeted compounds of the invention, especially finallytowards the compound 2,3,3,3-tetrafluoropropene (1234yf). For example,the chemistry to produce compound 243db is shown in Step 1 (CarbeneReaction) of Scheme 1 further below in the Detailed Description of theInvention. For example, the chemistry to produce compound 1234yf out ofcompound 243db is shown in Step 2 (Addition/Elimination Reaction) ofScheme 1 further below in the Detailed Description of the Invention.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows an example embodiment of the process according to theinvention and the synthesis of the compound 1234yf out of the compound123 as the initial starting material, and performed as a reactionsequence in two microreactors.

FIG. 2 shows an example embodiment of the process according to theinvention and the synthesis of the compound 1234yf out of the compound125 as the initial starting material, and performed as a reaction in amicroreactor.

DESCRIPTION OF THE PREFERRED EMBODIMENTS Definitions

Compounds in the context of the invention: The compound “1234yf” is2,3,3,3-tetrafluoropropene. The compound “243db” is2,3-dichloro-1,1,1-trifluoropropane. The compound “123” or “HCFC 123” is2,2-dichloro-1,1,1-trifluoroethane. The compound “124” is2-chloro-1,1,1,2-tetrafluoroethane. The compound “125” ispentafluoroethane. The compound “1233xf” is2-chloro-1,1,1-trifluoropropene. The compound “244bb” is2-chloro-1,1,1,2-tetrafluoropropane.

The term “liquid medium” or “liquid phase” may mean a solvent whichinert to fluorination under the reaction conditions of the directfluorination, in which the starting compound and/or fluorinated targetcompound may be dissolved, and/or the starting compound itself may be aliquid serving itself as liquid medium or liquid phase, and in which thefluorinated target compound may be dissolved if it is not a liquid, orif it is a liquid may also serve as the liquid medium or liquid phase.

The terms “comprising,” “including,” “having,” and their derivatives,are not intended to exclude the presence of any additional component,step or procedure, whether or not the same is specifically disclosed. Inorder to avoid any doubt, all compositions claimed through use of theterm “comprising” may include any additional additive, adjuvant, orcompound, whether polymeric or otherwise, unless stated to the contrary.In contrast, the term, “consisting essentially of” excludes from thescope of any succeeding recitation any other component, step, orprocedure, excepting those that are not essential to operability. Theterm “consisting of” excludes any component, step, or procedure notspecifically delineated or listed. The term “or,” unless statedotherwise, refers to the listed members individually as well as in anycombination. Use of the singular includes use of the plural and viceversa.

The term “vol.-%” as used herein means “% by volume”.

The term “wt.-%” as used herein means “% by weight”. Unless otherwisestated, all percentages (%) as used herein denote “wt.-%” or “% byweight”, respectively.

Any pressure value or range of pressure values given herein in, i.e.,“bar”, unless otherwise stated refer to “bar absolute” (abs.).

The numerical ranges disclosed herein include all values from, andincluding, the lower and upper value. For ranges containing explicitvalues (e.g., 1 to 7), any subrange between any two explicit values isincluded (e.g., 1 to 2; 2 to 6; 5 to 7; 3 to 7; 5 to 6; etc.).

The term “tube-like” is synonymous to the term “pipe-like” and viceversa.

As briefly described in the Summary of the Invention, and defined in theclaims and further detailed by the following description and examplesherein, the invention is particularly directed to processes ofmanufacturing the compound 2,3,3,3-tetrafluoropropene (1234yf), which isthe newest refrigerant with zero OPD (Ozone Depleting Potential) andzero GWP (Global Warming Potential), and of further compounds such asthe compound 2,3-dichloro-1,1,1-trifluoropropane (243db), which canserve as a starting material in the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf), and optionally of the compound2-chloro-1,1,1-trifluoropropene (1233xf); and wherein the processes ofthe present invention have in common that the manufacture of thecompounds involve at least one carbene generation step, e.g., asdescribed in the Summary of the Invention above.

Thus, the invention in particular relates to a process for themanufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf), and ofthe compound 2,3-dichloro-1,1,1-trifluoropropane (243db). The inventionalso relates to a process for the manufacture of the compound2,3,3,3-tetrafluoropropene (1234yf), wherein the compound2,3-dichloro-1,1,1-trifluoropropane (243db) serves as a startingmaterial. Further, the invention relates to a process for themanufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf), of thecompound 2,3-dichloro-1,1,1-trifluoropropane (243db), and optionally ofthe compound 2-chloro-1,1,1-trifluoropropene (1233xf), wherein theinitial starting materials are selected from the group consisting ofcompound 123 (2,2-dichloro-1,1,1-trifluoroethane), compound 124(2-chloro-1,1,1,2-tetrafluoroethane), and compound 125(pentafluoroethane). The compound 123(2,2-dichloro-1,1,1-trifluoroethane is preferred as the initial startingmaterial. In particular, the process of the invention involves a carbenegeneration step, and wherein the carbene formed is further reactedtowards the targeted compounds of the invention, especially finallytowards the compound 2,3,3,3-tetrafluoropropene (1234yf).

The present invention pertaining in particular to a novel process ofmanufacturing the compound 2,3,3,3-tetrafluoropropene (1234yf), which isthe newest refrigerant with zero OPD (Ozone Depleting Potential) andzero GWP (Global Warming Potential), shall be described and exemplifiedin more detail hereinafter, e.g., by reference to, but not being limitedto, preferred embodiments of the invention.

New Process for the Synthesis of 1234yf:

According to the present invention it now was found, for example, thatCF₃—CHCl₂ (HCFC123) can be conveniently reacted to the compound 243db inhigh yields with CH₃C1 in a carbene reaction in a first step. Thechemistry to compound 243db is according to the reaction step 1 inScheme 1 below, which is a carbene reaction step.

The compound 243db resulting from the first step, then in a second stepis further reacted to yield the compound 1234yf. The chemistry startingfrom compound 243db to provide the compound 1234yf is according reactionstep 2 in Scheme 1 below, which is an addition/elimination reactionstep.

The novel process of manufacturing the compound2,3,3,3-tetrafluoropropene (1234yf) according to the present inventionis a two-step process involving in a first step a carbene reaction,starting from HCFC 123 (2,2-dichloro-1,1,1-trifluoroethane) as startingcompound in the first step, and reacting the carbene compound formed,e.g., formed in situ, as exemplified with methyl chloride (CH₃C1) andelimination of HCl (hydrogen chloride), to produce the compound2,3-dichloro-1,1,1-trifluoropropane (243db) as the reaction product ofthe first step. Note: The invention is exemplified with methyl chloride(CH₃C1), but can analogously, for example, be also performed with anyother methyl halogenide compound of the formula CH₃X, as defined abovein the Summary of the Invention.

The compound 2,3-dichloro-1,1,1-trifluoropropane (243db) may eithersubsequently, e.g., without or with intermediate purification, stored inan intermediate storage tank, or directly be further reacted in thesecond step of the process to produce the compound2,3,3,3-tetrafluoropropene (1234yf), or optionally to produce thecompound 1233xf (2-chloro-1,1,1-trifluoropropene), or if desired, may beisolated and/or purified, e.g., as product on its own or for differentpurpose or application.

The carbene reaction in the first process step of manufacturing thecompound 2,3,3,3-tetrafluoropropene (1234yf) according to the presentinvention can be performed by two methods, as exemplified with methylchloride (CH₃C1):

-   -   Method 1A: Carbene generation in liquid phase with phase        transfer catalyst and base, and reaction with methyl chloride        (CH₃C1) and elimination of HCl (hydrogen chloride); or    -   Method 1B: Carbene generation in gas phase, high temperature        thermolysis, and reaction with methyl chloride (CH₃C1) and        elimination of HCl (hydrogen chloride).

The said carbene reaction in the said first process step of invention isexemplified with methyl chloride (CH₃C1), but can analogously, forexample, be also performed with any other methyl halogenide compound ofthe formula CH₃X, as defined above in the Summary of the Invention.

In the second step the compound 2,3-dichloro-1,1,1-trifluoropropane(243db) formed in the carbene reaction of the first step, then isreacted involving an addition reaction of HF (hydrogen fluoride) andelimination of HCl (hydrogen chloride), to produce the compound2,3,3,3-tetrafluoropropene (1234yf), or optionally to produce thecompound the compound 1233xf (2-chloro-1,1,1-trifluoropropene). Theaddition reaction in the second process step of manufacturing thecompound 2,3,3,3-tetrafluoropropene (1234yf) according to the presentinvention can be performed by two methods:

-   -   Method 2A: Addition reaction of HF (hydrogen fluoride) and        elimination of HCl (hydrogen chloride), both in liquid phase,        and induced by Lewis acid; or    -   Method 2B: Addition reaction of HF (hydrogen fluoride) and        elimination of HCl (hydrogen chloride), both in gas phase in the        presence of a, fluorination and/or halogenation, catalyst.

The novel process of manufacturing the compound2,3,3,3-tetrafluoropropene (1234yf) according to the present inventionis a two-step process, for example, which is shown in the followingScheme 1.

The process of the invention, alternatively to starting from compound123, can also be performed, starting from the compound 124(2-chloro-1,1,1,2-tetrafluoroethane) or the compound 125(pentafluoroethane), and is also involving the carbene generation in thefirst step of the process according to the present invention.

The compound 124 (chlorotetrafluoroethane) converted under the inventiveconditions gave 1234yf directly but 124 as starting material is lessconveniently available in large industrial scale. See Scheme 2.

But the compound 125 is produced in large industrial scale andconveniently available, e.g., by the reaction as shown in Scheme 3.

The reaction starting from 124 and also 125 proceeded in a Ni-tubereactor heated to 850° C. but conversion rates with 125 were around 50%lower (carbene generation) rate compared to 123 as starting material. Inprinciple, but not economic feasible—due to needed deep temperatures—isthe preparation of the suitable precursors CF₃—CF:—carbene out of 125 orCF₃—CCl:—carbene out of 124 over the corresponding Lithium salts whichpreparation is described by Kazakova, Olesya; Roeschenthaler,Gerd-Volker in “Efficient Preparations of Fluorine Compounds” (2013),205-209, but never used for 1234yf preparation, mentioned here for(scientific) complete information reason only.

However, as compared to the processes shown in Scheme 2 (for compound124 as initial starting material) and in Scheme 3 (for compound 125,preferred over compound 124, as initial starting material), the processof the invention, starting from compound 123(2,2-dichloro-1,1,1-trifluoroethane), and involving the carbenegeneration in the first step of the process according to the presentinvention, is particularly preferred. See Scheme 1 above.

New process for the synthesis of 1233xf:

According to the present invention it was also found that CF₃—CHCl₂(HCFC 123) can be conveniently reacted to the compound 1233xf in highyields with CH₃C1 involving a carbene reaction in a first step, asdescribed above, and also applicable in context of producing thecompound 1233xf. For example, in a simple tube reactor, the reactioncannot be stopped at compound 243db stage, and 2 mol equivalents of HClare eliminated. The chemistry to compound 1233xf is according to thereaction step 1 in Scheme 4 below.

The compound 1233xf resulting from the first step, then in a second stepis further reacted to yield the compound 1234yf. The chemistry startingfrom compound 1233xf to compound 1233xf to provide the compound 1234yfis according reaction step 2 in Scheme 4 below.

This process of manufacturing the compound 2,3,3,3-tetrafluoropropene(1234yf) via the compound 1233xf, is also a two-step process involvingin a first step a carbene reaction according to the invention, asdescribed above in the Summary of the Invention, starting from, e.g.,HCFC 123 (2,2-dichloro-1,1,1-trifluoroethane) as starting compound inthe first step, and reacting the carbene compound formed, e.g., formedin situ, for example, with methyl chloride (CH₃C1) and elimination ofHCl (hydrogen chloride), to produce the compound 1233xf(2-chloro-1,1,1-trifluoropropene) as the reaction product of the firststep.

The compound 1233xf (2-chloro-1,1,1-trifluoropropene) may eithersubsequently, e.g., without or with intermediate purification, stored inan intermediate storage tank, or directly be further reacted in thesecond step of the process to produce the compound2,3,3,3-tetrafluoropropene (1234yf), or, if desired, the compound 1233xf(2-chloro-1,1,1-trifluoropropene) may be isolated and/or purified, e.g.,as product on its own or for different purpose or application.

Accordingly, the invention may also relate to a novel process ofmanufacturing the compound 2-chloro-1,1,1-trifluoropropene (1233xf),involving a carbene reaction step according to the present invention,for example, via the intermediate, or in particular in situ, compound243db, for example, via the carbene route in a process which is shown inthe following Scheme 5.

Method 1A and 1B (Carbene Generation):

In chemistry, a carbene is a molecule containing a neutral carbon atomwith a valence of two and two unshared valence electrons. The generalformula is R—C(:)—R′ or R═C(:) where the R and R′ represent organiccarbon substituents or hydrogen atoms, and (:) represents two unsharedvalence electrons of the carbon atom (C). Reference is made to theSummary of the Invention, and the carbene generation step, e.g., asdescribed therein, and as applicable in the context of the processes ofthe invention, and which here shall be further detailed for the purposeof the invention.

Generation of carbenes can be achieved by several methods known in thestate of the art. In the context of the present invention, as indicatedherein above, the carbene compound is either generated in liquid phasewith phase transfer catalyst and base (Method 1A), or the carbenecompound is generated in gas phase by high temperature thermolysis(Method 1B).

Carbenes are reactive and usually formed as intermediates only, and thusreact further with suitable reactant compounds, e.g., in context of thepresent invention the reactant compound is, for example, methyl chloride(CH₃C1). The said carbene reaction in the said first process step ofinvention is exemplified with methyl chloride (CH₃C1), but cananalogously, for example, be also performed with any other methylhalogenide compound of the formula CH₃X, as defined above in the Summaryof the Invention.

Method 1A:

Carbene generation in liquid phase with phase transfer catalyst andbase.

In the context of the present invention the carbene compound is formed,in a method 1A, by base-induced elimination HX from haloforms (R—CHX₂,wherein X denotes a halogen, e.g. especially chlorine, Cl) underphase-transfer conditions, e.g., using a PTC (phase-transfer catalyst).

The haloform employed in context of the present invention for generatinga carbene of interest in the processes of manufacturing compoundsaccording to the objects of the invention, is a trifluoroethane compoundof the formula CF₃—CHX_(n)Y_(2-n), as defined above in the Summary ofthe Invention, for example, but not limited to, trifluoromethylchloride.

In chemistry, a phase-transfer catalyst or PTC is a catalyst thatfacilitates the migration of a reactant from one phase into anotherphase where reaction occurs. Phase-transfer catalysis is a special formof heterogeneous catalysis. Ionic reactants are often soluble in anaqueous phase but insoluble in an organic phase in the absence of thephase-transfer catalyst. The catalyst functions like a detergent forsolubilizing the salts into the organic phase. Phase-transfer catalysisrefers to the acceleration of the reaction upon the addition of thephase-transfer catalyst.

By using a PTC process, one can achieve faster reactions, obtain higherconversions or yields, make fewer by-products, eliminate the need forexpensive or dangerous solvents that will dissolve all the reactants ina single phase, eliminate the need for expensive raw materials and/orminimize waste problems. Phase-transfer catalysts are especially usefulin green chemistry, by allowing the use of water, the need for organicsolvents is reduced.

Contrary to common perception, PTC is not limited to systems withhydrophilic and hydrophobic reactants. PTC is sometimes employed inliquid/solid and liquid/gas reactions. As the name implies, one or moreof the reactants are transported into a second phase which contains bothreactants.

In the state of the art, several types of PTC process are known. Forexample, phase-transfer catalysts for anionic reactants are oftenquaternary ammonium salts. Commercially important phase-transfercatalysts include, for example, but are not limited to,benzyltriethylammonium chloride, methyltricaprylammonium chloride,methyltributylammonium chloride, and methyltrioctylammonium chloride.Organic phosphonium salts are also used for example, but are not limitedto, hexadecyltributylphosphonium bromide. The phosphonium salts toleratehigher temperatures, but may be unstable toward base, then degrading tophosphine oxide.

It was demonstrated that many carbene reactions can be performed rapidlyat around room temperature using catalysts such as tetra-n-butylammoniumbromide and methyltrioctylammonium chloride in benzene/water systems.

An alternative to the use of “quaternary salts” is to convert alkalimetal cations into hydrophobic cations. In the research lab, crownethers are used for this purpose. Polyethylene glycols are more commonlyused in practical applications. These ligands encapsulate alkali metalcations (typically Na⁺ and K⁺), affording large lipophilic cations.These polyethers have a hydrophilic “interiors” containing the ion and ahydrophobic “exterior”.

According to the present invention the carbene generation is performedin liquid phase with phase transfer catalyst and base. For generalinformation see M. Makosza, Pure Appl. Chem., Vol. 72, No. 7, pp.1399-1403, 2000.

The phase transfer catalyst may comprise a compound of at least one ofthe compound classes of, for example: a) linear or cyclic ammoniumsalts, b) heterocyclic ammonium salts, c) non-ionic phase transfercompounds, d) phosphonium salts, and combinations thereof. Examples, butnot intended to be limited thereto, are for the said compound classesare:

a) Ammonium salts like: benzalkoniumchloride (CAS Number: 63449-41-2),benzyldimethylhexylammonium chloride (CAS Number: 22559-57-5),2-bromoethyl)trimethylammonium bromide (CAS Number: 2758-06-7),hexyltrimethylammonium bromide, (CAS Number: 2650-53-5), andtetrabutylammonium bromide (CAS Number: 1643-19-2); and the commerciallyphase-transfer catalysts already mentioned above, for example, includingbenzyltriethylammonium chloride, methyltricaprylammonium chloride,methyltributylammonium chloride, and methyltrioctylammonium chloride.

b) Heterocyclic ammonium salts like: 1-butyl-2,3-dimethylimidazoliumchloride (CAS Number: 98892-75-2), hexadecylpyridinium bromide (CASNumber: 140-72-7), and 1-methylimidazolium hydrogen sulfate (CAS Number:681281-87-8);

c) Non-ionic phase transfer compounds: like DL-α-tocopherolmethoxypolyethylene glycol succinate (CAS Number: 1309573-60-1); and

d) Phosphonium salts like: tetrabutylphosphonium bromide (CAS Number:3115-68-), methyltriphenoxyphosphonium iodide (CAS Number: 17579-99-6),tetrabutylphosphoniummethanesulfonate (CAS Number: 98342-59-7),tetraphenylphosphonium bromide (CAS Number: 2751-90-8),trihexyltetradecylphosphonium bromide (CAS Number: 654057-97-3), andtrihexyltetradecylphosphonium chloride (CAS Number: 258864-54-9); andhexadecyltributylphosphonium bromide, a commercially phase-transfercatalysts already mentioned above.

The liquid phase may comprise as a solvent, e.g., any inert solvent orcombinations thereof. Examples, but not intended to be limited thereto,including mixtures of solvents are, e.g., trichloromethyl toluene,CH₂Cl₂ (methylene dichloride), toluene, DMF, DMSO, ethylene glycol,water (H₂O), butyrolactone. As accelerator, some crown ether can beadded as well, e.g., such crown ethers as known to the person skilled inthe art.

In chemistry, a base is, for example, (i) an inorganic substance thatcan accept hydrogen ions (protons, H⁺). Such a base may be an inorganicsubstance, including but not limited to, KOH, NaOH, LiOH, Ca(OH)₂, orcombinations thereof. Hence, in chemistry, bases (i) are substancesthat, in aqueous solution, release hydroxide (OH⁻) ions, are slippery tothe touch, can taste bitter if an alkali, change the color of indicators(e.g., turn red litmus paper blue), react with acids to form salts,promote certain chemical reactions (base catalysis), accept protons (H⁺)from any proton donor or contain completely or partially displaceableOH⁻ ions. Examples of bases are the hydroxides of the alkali metals andthe alkaline earth metals (NaOH, Ca(OH)₂, etc.; see alkali hydroxide andalkaline earth hydroxide). In water, by altering the autoionizationequilibrium, bases yield solutions in which the hydrogen ion activity islower than it is in pure water, i.e., the water has a pH higher than 7.0at standard conditions. A soluble base is called an alkali if itcontains and releases OH⁻ ions quantitatively. However, it is importantto realize that basicity is not the same as alkalinity. Metal oxides,hydroxides, and especially alkoxids are basic, and conjugate bases ofweak acids are weak bases.

In chemistry, a base is, for example, (ii) a metal organic substance,including but not limited to, Li-organyl compounds, alkali metals likeNa and K, or combinations thereof.

The base may comprise a solvent compatible with the respective base,e.g., with KOH, NaOH, LiOH, Ca(OH)₂, on the one hand, and, e.g., withLi-organyl compounds, alkali metals like Na and K, on the other hand.Examples of suitable solvents for the said bases, but not intended to belimited thereto, are water (H₂O) which is good for NaOH, KOH, LiOH, andCa(OH)₂; hexane, cyclohexane for Li-organyl compounds like Bu-Li (butyllithium), Me-Li (methyl lithium), and alkali metals like Na and K.

For example, the Method 1A process of the invention can be for themanufacture of the compound 1233xf (2-chloro-1,1,1-trifluoropropene),wherein the compound 1233xf is prepared in liquid phase under transfercatalysis reaction out of the compound 123(2,2-dichloro-1,1,1-trifluoroethane). See for example, EmbodimentExemplification 3.

Method 1B:

Carbene generation in gas phase by high temperature thermolysis.

In the context of the present invention the carbene compound is formed,in a method 1B, by high temperature thermolysis of haloforms (R—CHX₂,wherein X denotes a halogen, e.g. especially chlorine, Cl).

The haloform employed in context of the present invention for generatinga carbene of interest in the processes of manufacturing compoundsaccording to the objects of the invention, is a trifluoroethane compoundof the formula CF₃—CHX_(n)Y_(2-n), as defined above in the Summary ofthe Invention, for example, but not limited to, trifluoromethylchloride.

Thermolysis, or thermal decomposition, is a chemical decompositioncaused by heat. The decomposition temperature of a substance is thetemperature at which the substance chemically decomposes. The reactionis usually endothermic as heat is required to break chemical bonds inthe compound undergoing decomposition.

High temperature thermolysis, denotes a thermal decomposition at atemperature of about at least 400° C. For example, in the presentinvention the high temperature thermolysis is performed at a temperaturein the range of about 400° C. to about 950° C. Preferably, the hightemperature thermolysis is performed at a temperature in the range ofabout 500° C. to about 900° C. More preferably, the high temperaturethermolysis is performed at a temperature in the range of about 700° C.to about 800° C.

For example, the Method 1B process of the invention can be for themanufacture of the compound 1233xf (2-chloro-1,1,1-trifluoropropene),wherein the compound 1233xf is prepared in a gas phase (vapor phase)reaction out of the compound 123 (2,2-dichloro-1,1,1-trifluoroethane),preferably in a continuous reaction, more preferably in a continuousreaction in a Monel-tube reactor. See for example, EmbodimentExemplification 1.

For example, the Method 1B process of the invention can be for themanufacture of the compound 1233xf (2-chloro-1,1,1-trifluoropropene),wherein the compound 1233xf is prepared in a gas phase (vapor phase)reaction out of the compound 123 (2,2-dichloro-1,1,1-trifluoroethane),preferably in a continuous reaction, more preferably in a continuousreaction in a quartz glass tube reactor. See for example, EmbodimentExemplification 2.

Method 2A and Method 2B (addition/elimination reaction):

The addition reaction in the second process step of manufacturing thecompound 2,3,3,3-tetrafluoropropene (1234yf) according to the presentinvention can be performed by two methods:

-   -   Method 2A: Addition reaction of HF (hydrogen fluoride) and        elimination of HCl (hydrogen chloride), both in liquid phase,        and induced by Lewis acid; or    -   Method 2B: Addition reaction of HF (hydrogen fluoride) and        elimination of HCl (hydrogen chloride), both in gas phase        (vapor-phase) in the presence of a fluorination and/or        halogenation promoting catalyst.

For example, the chemistry to produce compound 1234yf out of compound243db, according to Method 2A or 2B is shown in Scheme 1 above, in Step2 (Addition/Elimination Reaction).

Details, as exemplification, for the Method 2A and Method 2B are givenfurther below.

Method 2A, Liquid Phase Fluorination/Addition with HF (Lewis Acid):

The Method 2A can be performed in the liquid phase, by the additionreaction of HF (hydrogen fluoride) and elimination of HCl (hydrogenchloride), both in liquid phase, and wherein the addition reaction of HFand elimination of HCl is induced by a Lewis acid.

In the process according to the invention, the Lewis acid in step(c)-(i), as this step is defined in claim 1, is a metal halogenide,preferable a metal halogenide selected from the group consisting ofSbCl₅/SbF₅, TiCl₄/TiF₄, SnCl₄/SnF₄, FeCl₃/FeF₃, ZnCl₂/ZnF₂, or is ahalogenation promoting catalyst, preferably fluorination promotingcatalyst, with Lewis acid properties.

Thus, suitable Lewis acids for the purpose of the present invention canalso be a fluorination and/or halogenation promoting catalyst,especially wherein the catalyst is a fluorination (promoting) catalyst,as described further below.

For example, the Method 2A process of the invention can be for themanufacture of the compound 1234yf (2,3,3,3-tetrafluoropropene), whereinthe compound 1234yf is prepared in liquid phase under transfer catalysisout of the compound 1233xf (2-chloro-1,1,1-trifluoropropene) byfluorination with anhydrous HF (hydrogen fluoride). The reaction can beperformed in an autoclave, e.g., with PTFE inliner. The Lewis acid maybe a fluorination and/or halogenation promoting catalyst, for example,SbCl_(x)F_(5-x). See for example, Embodiment Exemplification 4.

Method 2B, Gas Phase (Vapor-Phase) Fluorination/Addition with HF(Catalyst):

The Method 2A can be performed in in gas phase (vapor-phase), by theaddition reaction of HF (hydrogen fluoride) and elimination of HCl(hydrogen chloride), both in gas phase (vapor-phase), in the presence ofa fluorination and/or halogenation promoting catalyst, especiallywherein the catalyst is a fluorination (promoting) catalyst.

The gas phase (vapor-phase) fluorination process of the presentinvention is using gaseous hydrogen fluoride (HF) as the fluorinationgas. Most preferably, the gaseous hydrogen fluoride (HF) as thefluorination gas is “100%” gaseous hydrogen fluoride (HF), meaning thatthe gaseous hydrogen fluoride (HF) used is essentially consisting ofanhydrous gaseous hydrogen fluoride (anhydrous HF). The term “anhydrous”has the commonly applied technical meaning in the technical field ofchemistry. Accordingly, a substance is “anhydrous” if it contains nowater. Many processes in chemistry can be impeded by the presence ofwater. Therefore, it is important that water-free reagents andtechniques are used. In practice, however, it is very difficult toachieve absolute dryness; anhydrous compounds gradually absorb waterfrom the atmosphere so they must be stored and handled carefully toavoid such (re-)absorption of water. Techniques commonly known in thetechnical field of chemistry may be applied to prepare and to sustaingases, including gases of technical degree, essentially anhydrous.

The initial and/or preferred fluorination catalyst group of Cr-basedcatalysts used in the gas phase (vapor-phase) fluorination of thepresent invention, and used for preparing modifications of theseCr-based catalysts also used in the gas phase (vapor-phase) fluorinationof the present invention, were prepared according to the recipedisclosed by Dow in 1955 in said U.S. Pat. No. 2,745,886. Therefore,disclosure of said U.S. Pat. No. 2,745,886 is incorporated herein forthe purpose of the invention in its entirety.

The fluorination catalyst may be employed, for example in pelletizedform, as granules, or in form of a fluorination catalyst supported on acarrier, e.g., inorganic carrier, resistant to hydrogen fluoride (HF).Catalyst carrier may be also in form of pellets or granules, or may beany other support structure suitable to carry a gas phase (vapor-phase)catalyst, resistant to hydrogen fluoride (HF).

The gas phase (vapor-phase) fluorination process of the presentinvention can be performed as a batch process or as a continuousprocess. The skilled person will readily understand that additionalequipment has to be used, as applicable in a batch process or in acontinuous process, respectively, e.g., inlets, outlets, pipes,measurement equipment for pressure, temperature, flow-measurement andthe like, are employed as commonly known in the field of art, even ifnot specifically indicated herein below for reason of conciseness only.

In the process of the present invention particular focus preferably isput on a continuous gas phase (vapor-phase) fluorination process.Accordingly, also in case of a continuous gas phase (vapor-phase)fluorination step according to the present invention, the skilled personwill readily understand that additional equipment has to be used forsuch continuous gas phase (vapor-phase) fluorination, e.g., inlets,outlets, pipes, measurement equipment for pressure, temperature,flow-measurement and the like, as applicable, are employed as commonlyknown in the field of art, even if not specifically indicated hereinbelow for reason of conciseness only.

An exemplary apparatus for preparing, activating and/or re-activatingthe fluorination catalyst employed in the present invention, and/or forthe gas phase (vapor-phase) fluorination process of the presentinvention, for example, is a reactor consisting out of a Monel-tubefilled with catalyst pellets, a HF feeding system out of a stainlesssteel cylinder pressurized with N2 (dosage from liquid phase over aBronkhorst flow meter), a vaporizer operated at 180° C. for the feed tobe halogenated, a condenser with a reservoir after the tube reactorstill under slight overpressure, a scrubber just filled with water kept(cooled) at 25° C. and another scrubber filled with NaOH and a bubblecounter at the exit allowing exhaust gas and the N2 to exit.

For example, the Method 2B process of the invention is furtherexemplified below, for example, in the context of the Cr-basedcatalysts. The general gas-phase (vapor-phase) fluorination reactionwith hydrogen fluoride (HF) as fluorination gas and fluorinationcatalyst based on chromium, for example, Cr₂O₃, is as further describedherein below.

Methods with microreactor, applicable also to variant with coiledreactor:

According to a preferred embodiment of the present invention, thecompound 1234yf (2,3,3,3-tetrafluoropropene) can also be prepared in acontinuous manner out of the compound 123(2,2-dichloro-1,1,1-trifluoroethane). Preferably, this reaction isperformed in continuous manner. More preferably, the compound 1234yf(2,3,3,3-tetrafluoropropene) is prepared in a continuous manner out ofthe compound 123 (2,2-dichloro-1,1,1-trifluoroethane) in a twomicroreactor reaction. See for example, Embodiment Exemplification 5.

The, optionally intermediate, compound 243db(2,3-dichloro-1,1,1-trifluoropropane) produced in the firstmicroreactor, optionally may be isolated and/or purified, and then betransferred into the second microreactor to be further reacted byfluorination with anhydrous HF (hydrogen fluoride). The Lewis acid maybe a fluorination and/or halogenation promoting catalyst, for example,SbCl_(x)F_(5-x), as used for example, also in Embodiment Exemplification4.

The intermediate compound 243db (2,3-dichloro-1,1,1-trifluoropropane)produced in the first microreactor, optionally may be isolated and/orpurified, and then be the final product.

Preferably, intermediate compound 243db(2,3-dichloro-1,1,1-trifluoropropane) produced in the firstmicroreactor, as a crude compound 243db as obtained (e.g., not furtherpurified), is transferred into the second microreactor to be furtherreacted by fluorination with anhydrous HF (hydrogen fluoride). See forexample, Embodiment Exemplification 5. The Lewis acid may be afluorination and/or halogenation promoting catalyst, for example,SbCl_(x)F_(5-x), as used for example, also in Embodiment Exemplification4.

In a variant of the present invention, see for example, EmbodimentExemplification 6, the compound 1234yf (2,3,3,3-tetrafluoropropene) canalso be prepared out of the compound 125 (pentafluoroethane).Preferably, the reaction is performed in continuous manner. Morepreferably, the compound 1234yf (2,3,3,3-tetrafluoropropene) is preparedin a continuous manner out of the compound 125 (pentafluoroethane) in amicroreactor reaction, such as the first microreactor according toEmbodiment Exemplification 5.

In a further variant of the present invention, see for example,Embodiment Exemplification 7, the compound 1234yf(2,3,3,3-tetrafluoropropene) can also be prepared out of the compound243db (2,3-dichloro-1,1,1-trifluoropropane). The reaction can beperformed in the gas phase (vapor phase) by addition of HF (hydrogenfluoride), and elimination of HCl (hydrogen chloride). For example, thereaction is performed in two reaction zones (both zones as gas phase orvapor phase). In the first reaction zone an intermediate carbene isgenerated out of the compound 243db, over a catalyst, and theintermediate carbene compound generated out of the compound 243db isfurther reacted by fluorination with anhydrous HF (hydrogen fluoride).Preferably, the catalyst is a chromium-based catalyst, preferably aZn-doped chromium-based catalyst, e.g., Zn-doped chromium oxide (Cr₂O₃).The HCl formed in the first reaction zone, together with any residualHF, is stripped off in a cyclone, before the reaction product from thefirst zone enters the second reaction zone containing AlF3, preferablyAlF3 in form of pellets. The reaction can be performed in a Monel-tubereactor, providing the two reaction zones. Preferably, the reaction canbe performed in a continuous manner.

Fluorination Catalyst, Optionally with Lewis Acid Properties:

The processes of the invention employ a halogenation catalyst,preferably a fluorination catalyst. Halogenation is a chemical reactionthat involves the addition of one or more halogens to a compound ormaterial. The pathway and stoichiometry of halogenation depends on thestructural features and functional groups of the organic substrate, aswell as on the specific halogen. Inorganic compounds such as metals alsoundergo halogenation. Fluorination is a halogenation wherein F(fluorine) is the halogen introduced into a compound or material.Halogenation and/or fluorination are well known to those skilled in theart, as well as the halogenation catalysts and/or fluorination catalystsinvolved in these reactions. For example, the addition of halogens, e.g.chlorine and/or fluorine, to alkenes proceeds via intermediate haloniumions as an active species, wherein “halonium ion” in organic chemistrydenotes any onium compound (ion) containing a halogen atom, e.g. hereinin context of the invention a fluorine atom, carrying a positive charge.

Halogenation catalysts and/or fluorination catalysts are well known tothose skilled in the field, and preferably in context of the invention,based on Sb, As, Bi, Al, Zn, Fe, Mg, Cr, Ru, Sn, Ti, Co, Ni, preferablyon the basis of Sb.

The invention relates to a process, for example, wherein the catalyst isa halogenation catalyst, preferably a fluorination catalyst, on thebasis of Sb, As, Bi, Al, Zn, Fe, Mg, Cr, Ru, Sn, Ti, Co, Ni, preferablyon the basis of Sb, more preferably a fluorination catalyst, wherein thefluorination catalyst is selected from the group consisting of Sbfluorination catalysts providing the active species H₂F⁺SbF⁶⁻.

The invention relates to a process, for example, wherein thehalogenation catalyst is antimony pentachloride and/or antimonypentafluoride, preferably wherein the catalyst is antimony pentafluoride(SbF₅) and is prepared in an autoclave by reaction of SbCl₅ with HF,more preferably consisting of SbF₅ in HF which forms the active speciesH₂F⁺SbF⁶⁻, prior to reaction step (d) in the process according to anyone of embodiments (1) to (3).

In particular, the invention pertains to a first process (process 1) forthe manufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf)comprising the steps of:

(a) providing the compound 243db (2,3-dichloro-1,1,1-trifluoropropane)as a starting material or intermediate material;

(b) providing (anhydrous) HF (hydrogen fluoride);

(c) mixing and reacting the compound 243db(2,3-dichloro-1,1,1-trifluoropropane) of (a) with the HF of (b), in areactor, wherein

-   -   (i) the reaction is performed by addition reaction of HF and        elimination of HCl (hydrogen chloride), both in liquid phase,        and induced by a Lewis acid; or    -   (ii) the reaction is performed by addition reaction of HF and        elimination of HCl (hydrogen chloride), both in gas phase        (vapor-phase) in the presence of a halogenation promoting        catalyst, preferably fluorination promoting catalyst;

(d) withdrawing the reaction mixture obtained in (c) from the saidreactor in (c) to yield a 2,3,3,3-tetrafluoropropene (1234yf) comprisingproduct, preferably a 2,3,3,3-tetrafluoropropene (1234yf) product;

(e) optionally withdrawing the HCl formed in the reactor in (c) as aneffluent from reaction mixture obtained in (d);

and

(f) optionally purifying and/or isolating the 2,3,3,3-tetrafluoropropene(1234yf) product obtained in (d), or optionally in (e), to yieldpurified and/or isolated 2,3,3,3-tetrafluoropropene (1234yf).

In particular, the invention pertains to a second process (process 2)for the manufacture of the compound 243db(2,3-dichloro-1,1,1-trifluoropropane) comprising the steps of:

(a) providing the compound HCFC 123 (2,2-dichloro-1,1,1-trifluoroethane)as a starting material;

(b) generating a carbene (CF₃—C(:)Cl) out of the compound HCFC 123(2,2-dichloro-1,1,1-trifluoroethane) provided under (a), wherein

-   -   (i) the carbene generation is performed in a liquid phase with a        phase transfer catalyst and a base; or    -   (ii) the carbene generation is performed in gas phase        (vapor-phase) by high temperature thermolysis;

(c) mixing and reacting the carbene (CF₃—C(:)Cl) formed in (b) withmethyl chloride (CH₃C1) and elimination of HCl (hydrogen chloride);

(d) withdrawing the reaction mixture obtained in (c) from the saidreactor in (c) to yield a 243db (2,3-dichloro-1,1,1-trifluoropropane)comprising product, preferably a 243db(2,3-dichloro-1,1,1-trifluoropropane) product;

(e) optionally withdrawing the HCl formed in the reactor in (c) as aneffluent from reaction mixture obtained in (d);

and

(f) optionally purifying and/or isolating the 243db(2,3-dichloro-1,1,1-trifluoropropane) product obtained in (d), oroptionally in (e), to yield purified and/or isolated 243db(2,3-dichloro-1,1,1-trifluoropropane).

In particular, the invention pertains to a third process (process 3) forthe manufacture of 2,3,3,3-tetrafluoropropene (1234yf) according to thefirst process of the invention, wherein in the step (a), as defined inthe first process of the invention, the compound 243db(2,3-dichloro-1,1,1-trifluoropropane) provided as a starting material orintermediate material is obtained by the process for the manufacture ofcompound 243db (2,3-dichloro-1,1,1-trifluoropropane) as defined in thesecond process of the invention.

In particular, the invention pertains to a forth process (process 4) forthe manufacture of the compound 1233xf (2-chloro-1,1,1-trifluoropropene)comprising the steps of:

(a) providing the compound HCFC 123 (2,2-dichloro-1,1,1-trifluoroethane)as a starting material;

(b) generating a carbene (CF₃—C(:)Cl) out of the compound HCFC 123(2,2-dichloro-1,1,1-trifluoroethane) provided under (a), wherein

-   -   (i) the carbene generation is performed in a liquid phase with a        phase transfer catalyst and a base; or    -   (ii) the carbene generation is performed in gas phase        (vapor-phase) by high temperature thermolysis;

(c) mixing and reacting the carbene (CF₃—C(:)Cl) formed in (b) withmethyl chloride (CH₃C1) and elimination of HCl (hydrogen chloride), andfurther dehydrochlorination (—HCl);

(d) withdrawing the reaction mixture obtained in (c) from the saidreactor in (c) to yield a 1233xf (2-chloro-1,1,1-trifluoropropene)comprising product, preferably a 1233xf(2-chloro-1,1,1-trifluoropropene) product;

(e) optionally withdrawing the HCl formed in the reactor in (c) as aneffluent from reaction mixture obtained in (d);

and

(f) optionally purifying and/or isolating the 1233xf(2-chloro-1,1,1-trifluoroprop ene) product obtained in (d), oroptionally in (e), to yield purified and/or isolated 1233xf(2-chloro-1,1,1-trifluoropropene).

In particular, the invention pertains to a fifth process (process 5) forthe manufacture of the compound 2,3,3,3-tetrafluoropropene (1234yf)comprising the steps of:

(a) providing as a starting material (i) the compound 124(2-chloro-1,1,1,2-tetrafluoroethane) and/or (ii) the compound 125(pentafluoroethane);

(b) generating a carbene (CF₃—C(:)F) out of (i) the compound 124(2-chloro-1,1,1,2-tetrafluoroethane) and/or (ii) the compound 125(pentafluoroethane) provided under (a), wherein

-   -   (i) the carbene generation (CF₃—C(:)F) is performed in a liquid        phase with a phase transfer catalyst and a base; or    -   (ii) the carbene generation (CF₃—C(:)F) is performed in gas        phase (vapor-phase) by high temperature thermolysis;

(c) mixing and reacting the carbene (CF₃—C(:)F) formed in (b) withmethyl chloride (CH₃C1) and elimination of HCl (hydrogen chloride);

(d) withdrawing the reaction mixture obtained in (c) from the saidreactor in (c) to yield a 2,3,3,3-tetrafluoropropene (1234yf) comprisingproduct, preferably a 2,3,3,3-tetrafluoropropene (1234yf) product;

(e) optionally withdrawing (i) any or (ii) any HF, as formed in thecarbene generation in (b), and the HCl formed in the reactor in (c), asan effluent from reaction mixture obtained in (d);

and

(f) optionally purifying and/or isolating the 2,3,3,3-tetrafluoropropene(1234yf) product obtained in (d), or optionally in (e), to yieldpurified and/or isolated 2,3,3,3-tetrafluoropropene (1234yf).

The invention comprises also a sixth process (process 6) according toany one of first or third process above, wherein the Lewis acid in step(c)-(i), as this step is defined in process 1, is a metal halogenide,preferable a metal halogenide selected from the group consisting ofSbCl₅/SbF₅, TiCl₄/TiF₄, SnCl₄/SnF₄, FeCl₃/FeF₃, ZnCl₂/ZnF₂, or is ahalogenation promoting catalyst, preferably fluorination promotingcatalyst, with Lewis acid properties.

The invention comprises also a seventh process (process 7) according toany one of first or third process above, wherein the halogenationpromoting catalyst, preferably fluorination promoting catalyst, in step(c)-(ii), as this step is defined in first process, or the halogenationpromoting catalyst, preferably fluorination promoting catalyst, withLewis acid properties, as defined in forth process, is a halogenationcatalyst, preferably a fluorination catalyst, on the basis of Sb, As,Bi, Al, Zn, Fe, Mg, Cr, Ru, Sn, Ti, Co, Ni, preferably on the basis ofSb, more preferably a fluorination catalyst, wherein the fluorinationcatalyst is selected from the group consisting of Sb fluorinationcatalysts providing the active species H₂F⁺SbF⁶⁻.

The invention comprises also a eights process according to invention,wherein the halogenation catalyst is antimony pentachloride and/orantimony pentafluoride, preferably wherein the catalyst is antimonypentafluoride (SbF₅), and preferably is prepared in an autoclave byreaction of SbCl₅ with HF, more preferably consisting of SbF₅ in HFwhich forms the active species H₂F⁺SbF⁶⁻.

The invention comprises also a ninth process according to any one ofprocess 2 to process 5, wherein the high temperature thermolysis in step(b)-(ii), as this step is defined in each of the processes 2 to 5,denotes a thermal decomposition performed at a temperature of about atleast 400° C.; preferably wherein the high temperature thermolysis isperformed at a temperature in the range of about 400° C. to about 950°C.; more preferably, the high temperature thermolysis is performed at atemperature in the range of about 500° C. to about 900° C.; still morepreferably, the high temperature thermolysis is performed at atemperature in the range of about 700° C. to about 800° C.

The invention comprises also a tenth process according to any one ofprocess 2 to process 5, wherein the phase transfer catalyst in step(b)-(i), as this step is defined in each of the processes 2 to 5,comprises or consists of a compound of at least one of the compoundclasses of a) linear or cyclic ammonium salts, b) heterocyclic ammoniumsalts, c) non-ionic phase transfer compounds, d) phosphonium salts, andcombinations thereof.

The invention comprises also a process according to any one of process 2to process 5, wherein the base in step (b)-(i), as this step is definedin each of the processes 2 to 5, comprises or consists of (i) aninorganic substance selected from the group consisting of KOH, NaOH,LiOH, Ca(OH)₂, or combinations thereof, or comprises or consists of (ii)a metal organic substance selected from the group consisting ofLi-organyl compounds, alkali metals like Na and K, or combinationsthereof.

The invention comprises also a process according to any one of theprocesses 1 and 3, wherein the halogenation promoting catalyst,preferably fluorination promoting catalyst, in step (c)-(ii), as thisstep is defined in process 1, is a fluorination catalyst is selectedfrom the group consisting of Cr₂O₃ based catalyst, MGF₂ based catalyst,SbCl₅/C based catalyst, and FeCl₃/C based catalyst.

The invention comprises also a process, wherein the fluorinationcatalyst is selected from the group consisting of MgF₂ based catalyst,SbCl₅/C based catalyst, and FeCl₃/C based catalyst, and wherein the saidcatalyst is pre-fluorinated with hydrogen fluoride (HF).

The invention comprises also a process, wherein the fluorinationcatalyst is selected from the group Cr₂O₃ based catalyst.

The invention comprises also a process, wherein the Cr₂O₃ based catalystis an activated and/or re-activated Cr₂O₃ based catalyst.

The invention comprises also a process according to, wherein theactivated and/or re-activated Cr₂O₃ based catalyst is activated and/orre-activated by treatment with an oxygen containing gas; and/or whereinthe Cr₂O₃ based catalyst, preferably the activated and/or re-activatedCr₂O₃ based catalyst, is pre-fluorinated with hydrogen fluoride (HF).

The invention comprises also a process, wherein the activated and/orre-activated Cr₂O₃ based catalyst is activated and/or re-activated bytreatment with Zn dopant, preferably by treatment with ZnCl₂ as dopant,by treatment with Ni dopant, preferably by treatment with NiCl₂ asdopant. The invention comprises also a process, wherein the activatedand/or re-activated Cr₂O₃ based catalyst is activated and/orre-activated by treatment with Ni dopant, preferably by treatment withNiCl₂ as dopant, and wherein the said Ni dopant activated and/orre-activated Cr₂O₃ based catalyst is supported on AlF₃ as a carrier.

The invention comprises also a process, wherein the activated and/orre-activated Cr₂O₃ based catalyst is activated and/or re-activated bytreatment with Mg dopant, preferably by treatment with Mg as dopant, andwherein the said Mg dopant activated and/or re-activated Cr₂O₃ basedcatalyst is additionally treated with carbon (C) to yield an activatedand/or re-activated Cr—Mg—C fluorination catalyst.

The invention comprises also a process, wherein at least one reactionstep, as defined in any of the steps (c)-(i) to (c)-(ii) in claim 1 orclaim 3, or as defined in any of the steps (b)-(i) to (b)-(ii) in eachof the processes 2 to 5, in the said reactors is performed in acontinuous flow reactor; optionally wherein (i) the continuous flowreactor is a pipe-like continuous flow reactor, preferentially withminimal lateral dimensions of about >5 mm, more preferentially apipe-like continuous flow reactor in coiled form (tube-like coiledreactor), or (ii) the continuous flow reactor is a microreactor,preferably with upper lateral dimensions of up to about ≤5 mm.

The invention comprises also a process, wherein the at least onereaction step in the said reactors is performed (i) in a continuous flowreactor that is a coiled continuous flow reactor; optionally wherein (i)the coiled continuous flow reactor is a coiled pipe-like continuous flowreactor, preferentially with minimal lateral dimensions of about >5 mm.

The invention comprises also a process, wherein the at least onereaction step in the said reactors is performed (ii) in a continuousflow reactor that is a microreactor, preferably with upper lateraldimensions of up to about ≤5 mm.

The invention comprises also a process, wherein the at least onereaction step is performed (ii) in a microreactorunder one or more ofthe following conditions:

-   -   flow rate: of from about 10 ml/h up to about 4001/h;    -   temperature: of from about 30° C. up to about 150° C.;    -   pressure: of from about 5 bar up to about 50 bar;    -   residence time: of from about 1 minute up to about 60 minutes.

The invention comprises also a process, wherein at least one of the saidcontinuous flow reactors, preferably at least one of the microreactors,is a SiC-continuous flow reactor, preferably independently is anSiC-microreactor.

PARTICULAR EMBODIMENTS OF THE INVENTION Embodiment Exemplification 1

Continuous synthesis of 1233xf out of HCFC-123 in a Monel-tube reactorin gas phase, for example, according to following reaction scheme:

The reaction can be performed in a Monel tube (with desired dimension),diameter and length), electrically heated, N2-flow during heating up,e.g., filled with about 1 cm Ni-fillings from company Raschig (Germany).The reactor temperature is e.g. at about 800° C., and the compound 123feed can be controlled with a Bronkhorst flow meter over a vaporizer(operated e.g. at about 100° C.) is adjusted to desired g/h (desiredmol/h) 123 feed, and another Bronkhorst flow meter is adjusted to anabout equimolar to slight excess g/h (mol/h) chloromethane feed out of agas cylinder into the Monel tube. The pressure is kept by a pressurevalve at e.g. about 2 bar abs. The gas stream leaving the reactor tubeis fed over a about 1 m cooled pipe (about +20° C.) of about 1 cmdiameter into a water scrubber (operated at about room temperature) toabsorb HCl and to hydrolyze little amounts of phosgene like sideproducts. A GC/GC-MS analysis of the gas steam leaving the scrubberindicates a quantitative conversion of 123 and selectivity to 1233xf ofabout 96%. The gas steam after the scrubber is condensed into astainless steel cylinder (fed inlet over a deep with deep) cooled toabout −78° C. with CO₂/EtOH.

Embodiment Exemplification 2

Continuous synthesis of 1233xf out of HCFC-123 at about 800° C. in aquartz glass tube reactor in gas phase.

A quartz tube (with desired dimension), diameter and length) withelectrical heating and a N2-flow during heating up, filled with about 1cm quartz glass fillings can be used. The reactor temperature is e.g. atabout 800° C., the 123 feed can be controlled with a Bronkhorst flowmeter over a vaporizer (operated e.g. at about 100° C.) is adjusted todesired g/h (desired mol/h) 123 feed, and another Bronkhorst flow meteris adjusted to an about equimolar to slight excess g/h (mol/h)chloromethane feed out of a gas cylinder. The pressure is kept by apressure valve at e.g. about 1.2 bar abs. The gas stream leaving thereactor tube is fed over an about 1 m cooled pipe (about +25° C.) ofabout 1 cm diameter into a water scrubber to absorb HCl and to hydrolyzepotential phosgene like side products and some unstable intermediatesand phosgenes. A GC/GC-MS analysis of the gas steam leaving the scrubberindicates about 81% conversion of 123 and selectivity to 1233xf of about89%. The gas stream after the scrubber is condensed into a stainlesssteel cylinder (fed inlet over a deep with deep) cooled to about −78° C.with CO₂/EtOH.

Embodiment Exemplification 3

Synthesis of 1233xf in liquid phase under phase transfer catalysis.

In a ml-sized Roth autoclave with deep pipe and gas outlet, a desired mlquantity of 123 (desired g, desired mol) is mixed with KOH pellets and adesired ml quantity deionized water together with a required quantity ofTBAB (tetrabutylammoniumbomide, quantity required to achieve phasetransfer condition) and the autoclave is closed. The autoclave is heatedto e.g. about 80° C. Afterwards, a g-quantity (mol-quantity) liquid 123(using a piston pump) and an about equimolar to slight excess g-quantity(mol-quantity) chloromethane (over a Bronkhorst flow meter out of a gascylinder) is fed together over the deep pipe into the autoclave and thepressure was kept at e.g. about 4 bar abs. with a pressure valveinstalled at the gas outlet of the autoclave. The gas stream leaving thereactor tube is fed over an about 1 m cooled pipe (about +25° C.) ofabout 1 cm diameter into a water scrubber to absorb still some presentHCl (most of the HCl remains in the autoclave). A GC/GC-MS analysis ofthe gas steam leaving the scrubber contains no 123 but mainly 1233xf.The gas stream after the scrubber is again condensed into a stainlesssteel cylinder (fed inlet over a deep pipe) cooled to about −78° C. withCO₂/EtOH.

Embodiment Exemplification 4

Fluorination of 1233xf in liquid phase to 1234yf, for example, accordingto following reaction scheme:

In a ml-sized Roth autoclave with PTFE inliner, a deep pipe and gasexit, a desired g-quantity (desired mol-quantity) of 1233xf is dissolvedin a desired ml-quantity anhydrous HF fed out of a HF cylinder. ThenSbF₅ (freshly prepared out of SbCl₅ (traces of Cl are not exchanged sothe catalyst is SbCl_(x)F_(5-x), preparation in another autoclave) isadded. The autoclave with all the raw materials and the Sb is heated fore.g. about 1 h to e.g. about 95° C. (pressure raised to e.g. about 10bar) and is slowly worked up after cooling down into ice water in aplastic washing bottle with deep pipe. The gas leaving the washingbottle is trapped into a stainless steel cylinder cooled to about −78°C. and consists out of 1234yf with traces of impurities only. Someunconverted 1233xf is found as second phase in the washing bottle. Theisolated yield for 1234yf is about 76%, the 1233xf found back in thewashing bottle indicated a conversion of about 79% and a selectivity to1234yf of about 98%.

Embodiment Exemplification 5

Continuous preparation of 1234yf out of 123 in a two microreactorreaction sequence.

This process according to the invention is exemplified in FIG. 1,showing the synthesis of the compound 1234yf out of the compound 123 asthe initial starting material, and performed as a reaction sequence intwo microreactors.

1st step, for example, according to following reaction scheme:

A first ml-sized microreactor made out of Nickel from company Innosyn BV(Geelen, Netherlands) for carbene generation (heated to about 700° C.,pressure kept at about 12 bar abs. by a pressure valve) and a secondml-sized microreactor made out of SiC from Chemtrix were installed andoperated in row. In a first step, HFC 243db is formed byCF₃—CC12:—carbene insertion (formed out of 123 which was fed as liquidinto microreactor) into chloromethane. In comparison to the simple tubereactor out of Nickel or quartz glass, the residence time in thismicroreactor is carefully adjusted so as zero 1233xf is formed andquantitative conversion of compound 123 is achieved. After cooling thegas stream leaving microreactor 1 to about 0° C., over an about 100 cmcoil (diameter about 1 cm) made out of Hastelloy C4, most of the formedHCl from first stage is stripped over a cyclone and liquid 243db iscollected.

2nd step, for example, according to following reaction scheme:

Crude HCFC 243db is not further purified and fed together as HF/Sb aboutmolar 20:1 mixture (Sb^(V)) into the second microreactor heated to about98° C., pressure kept at about 11 bar abs.

In microreactor 2, chlorine/fluorine exchange happens in situ followedby HCl-elimination catalyzed by the Lewis acid function of theSb-catalyst. Another (not drawn) coil cooler operated at about 0° C. andanother cyclone was applied after microreactor 2 to strip HCl. After thecyclone, the process stream entered a phase separator cooled to about−10° C. where a crude 1234yf gives the lower phase which is subjected toa continuous fine distillation. In a stainless steel column pure 1234yfat a transition temperature of about +35° C./about 10 bar abs. The upperphase of the separator is fed back into the HF/catalyst storage tank,about 5 mol-% (vs. Sb-concentration) of F₂ is added (Cl₂ also would bepossible) into the stream to convert some formed low reactive Sb^(III)back to the Sb^(V) oxidation state (some deactivation of Sb^(V)→Sb^(III)happens during fluorination).

In this procedure, for example, a g-sized (e.g., about 3.27 mol) 123 perhour, and for example, an about equimolar to slight excess (e.g., about166.6 g; e.g., about 3.3 mol) chloromethane per hour is reacted in twosteps in about 92% yield and full 123 conversion to 1234yf. In seldomcase of some traces of hydrolysable fluoride in the final distilledproduct, a further purification over NaF pellets can be applied.

Embodiment Exemplification 6

Synthesis of 1234yf out of 125 in microreactor, for example, accordingto following reaction scheme:

The installation is similar to that in Embodiment Exemplification 5 butonly the first microreactor made out of Nickel is used.

This process according to the invention is exemplified in FIG. 2,showing the synthesis of the compound 1234yf out of the compound 125 asthe initial starting material, and performed as a reaction in amicroreactor.

A g-size (e.g., about 360.1 g; e.g., about 3.0 mol) 125 per hour, and anabout equimolar to slight excess g-size (e.g., about 161.6 g; e.g.,about 3.2 mol) CH₃C1 per hour is fed over Bronkhorst flow meters and outof stainless steel cylinders each into the microreactor kept at, e.g.,about 12 bar abs. by a pressure valve. After the microreactor and thecoil cooler (e.g., about 1 m length; e.g., about d=1 cm) operated at,e.g., about 0° C., some HF with most of the formed HCl is leaving overthe cyclone. The product stream after the cyclone is all collected in acooling trap kept at about −78° C. An analysis of the gas phase of acarefully hydrolyzed sample out of that cylinder showed an about 75%conversion of 125 and selectivity to 1234yf of about 98%. The stainlesssteel column as described in Embodiment Exemplification 5 is used for afine distillation (at about 10 bar abs.) of material previously washedover ice water before distillation. The achieved 1234yf purity at atransition temperature of about 35° C. was about 99.9% (GC).

Embodiment Exemplification 7

Synthesis of 1234yf out of 243db in gas phase with Zn dopedCr₂O₃-catalyst over two reaction zones, for example, according tofollowing reaction scheme:

Apparatus: The 2 zone tube reactor system consists out of, for example,about 2×25 cm Monel-tube (for example, about diameter 5 cm). The firstzone is filled with Zn doped Cr₂O₃ catalyst pellets. A HF feeding systemis installed over a vaporizer and consists out of a stainless steelcylinder pressurized with N2 (dosage from liquid phase over a Bronkhorstflow meter into the vaporizer). The vaporizer is operated at, forexample, about 120° C. (needed for the 243db b.p. 77° C.). The zones areseparated by a cyclone where almost all HCl together with most of the HFis stripped out before the material enters the second zone. The secondzone (for example, about 25 cm) is filled with AlF₃ pellets (forexample, about d=2 mm) prepared out of commercial AlF₃ powder bypressing. The first zone is electrically heated to, for example, about150° C., the second zone to, for example, about 350° C.

Recipe for the preparation of the catalysts (given quantities andmeasures are for example only, and may be easily modified by the personskilled in the art):

Zn-doped Cr₂O₃ catalyst preparation: about 1 kg (about 19.2 mol) ofchromia in form of granules of size about 0.5 to about 1.4 mm andsurface of about 50 m²/g (Strem chemicals) was added to a solution ofabout 78.6 g (about 0.5769 mol) ZnCl₂ in about 11 distilled water andstirred for about 1 h at room temperature. Afterwards, the material wasdried in vacuum (about 20 mbar/about 60° C.) until no weight loss couldbe observed resulting in particles of size about 0.5 to about 1.4 mmwith about 3 wt.-% Zn. This catalyst was filled into the first zone ofthe reactor and pre-fluorinated about 2 h with an anhydrous HF streamuntil no water could be detected any more in the stream leaving thereactor. The AlF₃-pellets were just dried in N2-stream at about 350° C.before usage.

A g-size (e.g., about 250 g; e.g., about 1.50 mol) 243db per hour is fedtogether with an about five times equimolar to slight excess-size (e.g.,about 150 g; e.g., about 7.5 mol) anhydrous HF per hour over thevaporizer into zone 1 and after having passed a cyclone into zone 2. Thepressure was kept at about 10 bar by a pressure valve after reactor 2,another valve at the exit of the cyclone (operated at about 21° C.) wasadjusted to a material flow of about 31/minute into a scrubber system.The gas stream leaving reactor 2 was fed over another cyclone to stripHCl before it was collected into a cooling trap (at about −78° C.). Allmaterial collected in the cooling trap was carefully washed with icewater (washing bottle), the gas steam leaving the washing bottleindicated already a 1234yf crude material composition of about 98%besides some undefined % impurities. Isolated 1234yf is about 78% overthe two steps.

The Process of the Invention (Monel-Tube Reactor):

An exemplary apparatus for preparing, activating and/or re-activatingthe fluorination catalyst employed in the present invention, and/or forthe gas phase (vapor-phase) fluorination process of the presentinvention, for example, is a reactor consisting out of a Monel-tubefilled with catalyst pellets, a HF feeding system out of a stainlesssteel cylinder pressurized with N2 (dosage from liquid phase over aBronkhorst flow meter), a vaporizer operated at 180° C. for the startingmaterial feed, a condenser with a reservoir after the tube reactor stillunder slight overpressure, a scrubber just filled with water kept(cooled) at 25° C. and another scrubber filled with NaOH and a bubblecounter at the exit allowing exhaust gas and the N2 to exit.

For the gas phase (vapor-phase) fluorination process of the presentinvention, for example, the Monel tube (d=10 cm, volume around 6.51,electrically heated) is filled with a kg-scale quantity of thefluorination catalyst, for example at least 1 kg of the fluorinationcatalyst, preferably at least 2 kg, 3 kg, or 4 kg, more preferably atleast 5 kg, or even at least 6 kg, 7 kg, 8 kg or 9 kg of thefluorination catalyst. The Monel tube is (electrically) heated to thereaction temperature of at least about 200° C., preferably of at leastabout 250° C., more preferably to a reaction temperature of about 280°C., and then the feed into the monel tube, of HF feed and startingmaterial feed, was adjusted in relation to the employed kg-scalequantity of the fluorination catalyst, for example, based on 1 kg of thefluorination catalyst, the feed is adjusted to HF and starting materialfeed, both feeds fed over the vaporizer, which is operated at 180° C.for 1 h. Carefully hydrolyzed samples (see below), taken during thedescribed gas phase (vapor-phase) fluorination process of the presentinvention from the fluorination product reservoir, showed almostquantitative conversion. The reaction time can be adjusted in relationto the employed quantity of fluorination catalyst on the one hand, andthe quantity of HF feed and or starting material feed on the other hand.

It goes without saying that it is apparent to the person skilled in theart to also use any other reactor equipment suitable for catalytic gasphase reactions, fitted to be resistant to hydrogen fluoride (HF).

According to the vapor-phase fluorination process of the invention areaction temperature is to be achieved and sustained at a vapor-phasereaction temperature in a range of from about 200° C. to about 300° C.,preferably in a range of from about 250° C. to about 300° C., morepreferably in a range of from about 270° C. to about 290° C.; and forexample of about 280° C.

All materials, e.g., gas phase (vapor-phase) fluorination product,obtained in the gas phase (vapor-phase) fluorinations of the presentinvention leaving the reactors were collected by means of a condenserwith a (product) reservoir. After having finished the gas phase(vapor-phase) fluorination, the collected gas phase (vapor-phase)fluorination product is worked up, by hydrolysis, by pouring thecollected gas phase (vapor-phase) fluorination product very carefullyinto cooled water, preferably cooled water at a temperature of about 0°C. to about 10° C., more preferably cooled water at a temperature ofabout 0° C. to about 5° C. In a particular example, the gas phase(vapor-phase) fluorination product, obtained is carefully poured intoice water. The fluorinated product is further worked up by phaseseparation of the organic phase from the water phase, and optionally canbe further purified by distillation of the organic phase at atmosphericpressure, to obtain the purified product.

The Cr-based Catalysts:

The general gas-phase (vapor-phase) fluorination reaction with hydrogenfluoride (HF) as fluorination gas and fluorination catalyst based onchromium, for example, Cr₂O₃.

In the present invention the fluorination catalyst of the U.S. Pat. No.2,745,886 (1955) is analogously used for the gas-phase (vapor-phase)fluorination reaction step with hydrogen fluoride (HF) as fluorinationgas. Herein the hydrated chromium fluoride may be activated with oxygenas particularly described in the U.S. Pat. No. 2,745,886 (1955), andthat the catalyst material so activated is very effective in catalyzingthe vapor-phase fluorination reaction of the starting material andhydrogen fluoride (HF) as the fluorination gas. In fact, the catalystsare believed to be basic chromium fluorides, and more active than CrF₃.The said catalysts are also more effective in directing the course ofthe vapor-phase fluorination to greater conversions and yields of morehighly fluorinated products, and at much lower temperatures, than hasbeen achieved before.

In a particular embodiment of the present invention, the fluorinationcatalyst was prepared according to example 3 part B as described U.S.Pat. No. 2,745,886 starting with Cr₂O₃ (99% purity) and HF (anhydrous,100%) giving CrF₃×3 H₂O, and, after adding 2 wt.-% graphite andformation of pellets, the catalyst was activated with oxygen.

In analogy to example 3 part B as described U.S. Pat. No. 2,745,886, thecatalyst in accordance with the present invention was prepared bypassing a stream of oxygen through a bed of 3/16 inch by 3/16 inchdisc-shaped pellets containing 2 weight percent graphite preparedaccording to the following procedure:

-   -   A catalyst in accordance with the invention was prepared by        reacting high purity chromium trioxide (CrO₃) with an excess of        70 weight percent hydrofluoric acid. The semi-crystalline bright        green reaction product was heated in a drying oven at 80° C. to        sensible dryness. This sensibly dry product, consisting        preponderantly of α-CrF₃×3 H₂O was ground to pass through a 10        mesh screen, admixed with 2 weight percent graphite, and was        pressed into 3/16 inch by 3/16 inch disc-shaped pellets.

The dimensions of the catalyst bed and the conditions of the activationstep were the same as described in example 3 of U.S. Pat. No. 2,745,886,except that oxygen was employed instead of air, e.g., according to thefollowing procedure:

-   -   The catalyst pellets produced as described here-above were        packed to a height of about 12 inches in the 2 inch nickel        reaction tube as described in the examples of U.S. Pat. No.        2,745,886, or alternatively or preferably, into a Monel tube as        described herein-above and employed in in the context of the        present invention. The catalyst pellets were then activated by        heating them to, and holding them for two hours at, 500° C. in a        stream of oxygen. Of course, alternatively also air as described        in example of U.S. Pat. No. 2,745,886 can be used.

The Cr-based catalysts prepared above are amorphous to X-ray diffractionanalysis.

For example, the process of preparing a Cr-based fluorination catalystsfor use in the vapor-phase process of the present invention can beperformed such that the method of preparing a catalyst useful inpromoting the fluorination by vapor-phase reaction with hydrogenfluoride, said method comprising heating a mixture of a major proportionof hydrated chromium fluoride and a minor proportion of chromiumtrioxide at a temperature above about 400° C. for a time sufficientlylong to convert at least part of the hydrated chromium fluoride to abasic chromium fluoride.

For example, the process of preparing a Cr-based fluorination catalystsfor use in the vapor-phase process of the present invention can beperformed such that the method of preparing a catalyst useful inpromoting the fluorination by vapor-phase reaction with hydrogenfluoride, said method consisting essentially of heating a hydratedchromium fluoride to a temperature in the range of from about 350° to750° C. in the presence of oxygen.

For example, the process of preparing a Cr-based fluorination catalystsfor use in the vapor-phase process of the present invention can beperformed such that the method of preparing a catalyst useful inpromoting the fluorination by vapor-phase reaction with hydrogenfluoride, said method consisting essentially of heating a hydratedchromium fluoride to a temperature in the range of from about 350° C. toabout 650° C., while passing a: stream of a gas comprising molecularoxygen there through for a time sufficiently long for a small thougheffective amount of oxygen to react therewith.

For example, the process of preparing a Cr-based fluorination catalystsfor use in the vapor-phase process of the present invention can beperformed such that in the said process the gas stream is oxygen.

For example, the process of preparing a Cr-based fluorination catalystsfor use in the vapor-phase process of the present invention can beperformed such that in the said process the gas stream is air.

For example, the process of preparing a Cr-based fluorination catalystsfor use in the vapor-phase process of the present invention can beperformed such that the said method is comprising heating a bed ofCrF₃×3H₂O to an activation temperature in the range of from 350° to 650°C., while passing a stream of a gas comprising molecular oxygen therethrough, the flow of gas being maintained through said bed within saidactivation temperature range for a time sufficiently long to convert atleast part of the hydrated chromium fluoride to a basic chromiumfluoride.

For example, the process of preparing a Cr-based fluorination catalystsfor use in the vapor-phase process of the present invention can beperformed such that the said the CrF₃×3H₂O is the alpha hydrate.

Microreactor Process/Coiled Reactor Process:

The invention also may pertain to a process for the manufacture of afluorinated compound according to any of the preceding processes,wherein the process is a continuous process, preferably wherein thecontinuous process is carried out in a microreactor. The disclosureherein, throughout the application, is also applicable to coiledreactor, e.g., a tube-like coiled reactor (e.g., a tube reactor which isin coiled form). Hence, except for reactor dimensions, the datacontained herein for “microreactor” is also applicable to a coiledreactor, e.g., tube-like coiled reactor.

In general, the fluorination gas containing the hydrogen fluoride (HF)is fed into the microreactor in accordance with the requiredstoichiometry (sometimes with a slight excess) for the targetedfluorinated product and fluorination degree, and adapted to the reactionrate.

The invention may employ more than a single microreactor, i.e., theinvention may employ two, three, four, five or more microreactors, foreither extending the capacity or residence time, for example, to up toten microreactors in parallel or four microreactors in series. If morethan a single microreactor is employed, then the plurality ofmicroreactors can be arranged either sequentially or in parallel, and ifthree or more microreactors are employed, these may be arrangedsequentially, in parallel or both.

The invention is also very advantageous, in one embodiment wherein thedirect fluorination of the invention optionally is performed in acontinuous flow reactor system, or preferably in a microreactor system.

In an preferred embodiment the invention relates to a process for themanufacture of a fluorinated compound according to the invention,wherein the reaction is carried out in at least one step as a continuousprocesses, wherein the continuous process is performed in at least onecontinuous flow reactor with upper lateral dimensions of about ≤5 mm, orof about ≤4 mm,

preferably in at least one microreactor;

more preferably wherein of the said steps at least (b2) the step of afluorination reaction is a continuous process in at least onemicroreactor under one or more of the following conditions:

-   -   flow rate: of from about 10 ml/h up to about 4001/h;    -   temperature: of from about 30° C. up to about 150° C.;    -   pressure: of from about 4 bar up to about 50 bar;    -   residence time: of from about 1 second, preferably from about 1        minute, up to about 60 minutes.

In another preferred embodiment the invention relates to such a processof preparing a compound according to the invention, wherein at least oneof the said continuous flow reactors, preferably at least one of themicroreactors, independently is a SiC-continuous flow reactor,preferably independently is a SiC-microreactor.

The Continuous Flow Reactors and Microreactors/Coiled Reactors:

In addition to the above, according to one aspect of the invention, alsoa plant engineering invention is provided, as used in the processinvention and described herein, pertaining to the optional, and in someembodiments of the process invention, the process even preferredimplementation in microreactors and/or in coiled reactors. Hence, exceptfor reactor dimensions, the data contained herein for “microreactor” isalso applicable to a coiled reactor, e.g., tube-like coiled reactor.

As to the term “microreactor”: A “microreactor” or “microstructuredreactor” or “microchannel reactor”, in one embodiment of the invention,is a device in which chemical reactions take place in a confinement withtypical lateral dimensions of about ≤1 mm; an example of a typical formof such confinement are microchannels. Generally, in the context of theinvention, the term “microreactor”: A “microreactor” or “microstructuredreactor” or “microchannel reactor”, denotes a device in which chemicalreactions take place in a confinement with typical lateral dimensions ofabout ≤5 mm.

Microreactors are studied in the field of micro process engineering,together with other devices (such as micro heat exchangers) in whichphysical processes occur. The microreactor is usually a continuous flowreactor (contrast with/to a batch reactor). Microreactors offer manyadvantages over conventional scale reactors, including vast improvementsin energy efficiency, reaction speed and yield, safety, reliability,scalability, on-site/on-demand production, and a much finer degree ofprocess control.

Microreactors are used in “flow chemistry” to perform chemicalreactions.

In flow chemistry, wherein often microreactors are used, a chemicalreaction is run in a continuously flowing stream rather than in batchproduction. Batch production is a technique used in manufacturing, inwhich the object in question is created stage by stage over a series ofworkstations, and different batches of products are made. Together withjob production (one-off production) and mass production (flow productionor continuous production) it is one of the three main productionmethods. In contrast, in flow chemistry the chemical reaction is run ina continuously flowing stream, wherein pumps move fluid into a tube, andwhere tubes join one another, the fluids contact one another. If thesefluids are reactive, a reaction takes place. Flow chemistry is awell-established technique for use at a large scale when manufacturinglarge quantities of a given material. However, the term has only beencoined recently for its application on a laboratory scale.

Continuous flow reactors, e.g. such as used as microreactor, aretypically tube like and manufactured from non-reactive materials, suchknown in the prior art and depending on the specific purpose and natureof possibly aggressive agents and/or reactants. Mixing methods includediffusion alone, e.g. if the diameter of the reactor is narrow, e.g. <1mm, such as in microreactors, and static mixers. Continuous flowreactors allow good control over reaction conditions including heattransfer, time and mixing. The residence time of the reagents in thereactor, i.e. the amount of time that the reaction is heated or cooled,is calculated from the volume of the reactor and the flow rate throughit: Residence time=Reactor Volume/Flow Rate. Therefore, to achieve alonger residence time, reagents can be pumped more slowly, just a largervolume reactor can be used and/or even several microreactors can beplaced in series, optionally just having some cylinders in between forincreasing residence time if necessary for completion of reaction steps.In this later case, cyclones after each microreactor help to let formedHCl to escape and to positively influence the reaction performance.Production rates can vary from milliliters per minute to liters perhour.

Some examples of flow reactors are spinning disk reactors (ColinRamshaw); spinning tube reactors; multi-cell flow reactors; oscillatoryflow reactors; microreactors; hex reactors; and aspirator reactors. Inan aspirator reactor a pump propels one reagent, which causes a reactantto be sucked in. Also to be mentioned are plug flow reactors and tubularflow reactors.

In the present invention, in one embodiment it is particularly preferredto employ a microreactor.

In the use and processes according to the invention in a preferredembodiment the invention is using a microreactor. But it is to be notedin a more general embodiment of the invention, apart from the saidpreferred embodiment of the invention that is using a microreactor, anyother, e.g. preferentially pipe-like, continuous flow reactor with upperlateral dimensions of up to about 1 cm, and as defined herein, can beemployed. Thus, such a continuous flow reactor preferably with upperlateral dimensions of up to about ≤5 mm, or of about ≤4 mm, refers to apreferred embodiment of the invention, e.g. preferably to amicroreactor. Continuously operated series of STRs is another option,but less preferred than using a microreactor.

In the before said embodiments of the invention, the minimal lateraldimensions of the, e.g. preferentially pipe-like, continuous flowreactor can be about >5 mm; but is usually not exceeding about 1 cm.Thus, the lateral dimensions of the, e.g. preferentially pipe-like,continuous flow reactor can be in the range of from about >5 mm up toabout 1 cm, and can be of any value therein between. For example, thelateral dimensions of the, e.g. preferentially pipe-like, continuousflow reactor can be about 5.1 mm, about 5.5 mm, about 6 mm, about 6.5mm, about 7 mm, about 7.5 mm, about 8 mm, about 8.5 mm, about 9 mm,about 9.5 mm, and about 10 mm, or can be can be of any valueintermediate between the said values.

In the before said embodiments of the invention using a microreactorpreferentially the minimal lateral dimensions of the microreactor can beat least about 0.25 mm, and preferably at least about 0.5 mm; but themaximum lateral dimensions of the microreactor does not exceed about ≤5mm. Thus, the lateral dimensions of the, e.g. preferentialmicroreactorcan be in the range of from about 0.25 mm up to about ≤5 mm,and preferably from about 0.5 mm up to about ≤5 mm, and can be of anyvalue therein between. For example, the lateral dimensions of thepreferential microreactorcan be about 0.25 mm, about 0.3 mm, about 0.35mm, about 0.4 mm, about 0.45 mm, and about 5 mm, or can be of any valueintermediate between the said values.

As stated here before in the embodiments of the invention in itsbroadest meaning is employing, preferentially pipe-like, continuous flowreactor with upper lateral dimensions of up to about 1 cm. Suchcontinuous flow reactor, for example is a plug flow reactor (PFR).

The plug flow reactor (PFR), sometimes called continuous tubularreactor, CTR, or piston flow reactors, is a reactor used to perform anddescribe chemical reactions in continuous, flowing systems ofcylindrical geometry. The PFR reactor model is used to predict thebehaviour of chemical reactors of such design, so that key reactorvariables, such as the dimensions of the reactor, can be estimated.

Fluid going through a PFR may be modelled as flowing through the reactoras a series of infinitely thin coherent “plugs”, each with a uniformcomposition, traveling in the axial direction of the reactor, with eachplug having a different composition from the ones before and after it.The key assumption is that as a plug flows through a PFR, the fluid isperfectly mixed in the radial direction (i.e. in the lateral direction)but not in the axial direction (forwards or backwards).

Accordingly, the terms used herein to define the reactor type used inthe context of the invention such like “continuous flow reactor”, “plugflow reactor”, “tubular reactor”, “continuous flow reactor system”,“plug flow reactor system”, “tubular reactor system”, “continuous flowsystem”, “plug flow system”, “tubular system” are synonymous to eachother and interchangeably by each other.

The reactor or system may be arranged as a multitude of tubes, which maybe, for example, linear, looped, meandering, circled, coiled, orcombinations thereof. If coiled, for example, then the reactor or systemis also called “coiled reactor” or “coiled system”.

In the radial direction, i.e. in the lateral direction, such reactor orsystem may have an inner diameter or an inner cross-section dimension(i.e. radial dimension or lateral dimension, respectively) of up toabout 1 cm. Thus, in an embodiment the lateral dimension of the reactoror system may be in the range of from about 0.25 mm up to about 1 cm,preferably of from about 0.5 mm up to about 1 cm, and more preferably offrom about 1 mm up to about 1 cm.

In further embodiments the lateral dimension of the reactor or systemmay be in the range of from about >5 mm to about 1 cm, or of from about5.1 mm to about 1 cm.

If the lateral dimension at maximum of up to about ≤5 mm, or of up toabout ≤4 mm, then the reactor is called “microreactor”. Thus, in stillfurther microreactor embodiments the lateral dimension of the reactor orsystem may be in the range of from about 0.25 mm up to about ≤5 mm,preferably of from about 0.5 mm up to about ≤5 mm, and more preferablyof from about 1 mm up to about ≤5 mm; or the lateral dimension of thereactor or system may be in the range of from about 0.25 mm up to about≤4 mm, preferably of from about 0.5 mm up to about ≤4 mm, and morepreferably of from about 1 mm up to about ≤4 mm.

In an alternative embodiment of the invention, it is also optionallydesired to employ another continuous flow reactor than a microreactor,preferably if, for example, the (halogenation promoting, e.g. thehalogenation or preferably the halogenation) catalyst composition usedin the halogenation or fluorination tends to get viscous during reactionor is viscous already as a said catalyst as such. In such case, acontinuous flow reactor, i.e. a device in which chemical reactions takeplace in a confinement with lower lateral dimensions of greater thanthat indicated above for a microreactor, i.e. of greater than about 1mm, but wherein the upper lateral dimensions are about ≤4 mm.Accordingly, in this alternative embodiment of the invention, employinga continuous flow reactor, the term “continuous flow reactor” preferablydenotes a device in which chemical reactions take place in a confinementwith typical lateral dimensions of from about ≥1 mm up to about ≤4 mm.In such an embodiment of the invention it is particularly preferred toemploy as a continuous flow reactor a plug flow reactor and/or a tubularflow reactor, with the said lateral dimensions. Also, in such anembodiment of the invention, as compared to the embodiment employing amicroreactor, it is particularly preferred to employ higher flow ratesin the continuous flow reactor, preferably in the plug flow reactorand/or a tubular flow reactor, with the said lateral dimensions. Forexample, such higher flow rates, are up to about 2 times higher, up toabout 3 times higher, up to about 4 times higher, up to about 5 timeshigher, up to about 6 times higher, up to about 7 times higher, or anyintermediate flow rate of from about ≥1 up to about ≤7 times higher, offrom about ≥1 up to about ≤6 times higher, of from about ≥1 up to about≤5 times higher, of from about ≥1 up to about ≤4 times higher, of fromabout ≥1 up to about ≤3 times higher, or of from about ≥1 up to about ≤2times higher, each as compared to the typical flow rates indicatedherein for a microreactor. Preferably, the said continuous flow reactor,more preferably the plug flow reactor and/or a tubular flow reactor,employed in this embodiment of the invention is configured with theconstruction materials as defined herein for the microreactors. Forexample, such construction materials are silicon carbide (SiC) and/orare alloys such as a highly corrosion resistantnickel-chromium-molybdenum-tungsten alloy, e.g. Hastelloy®, as describedherein for the microreactors.

A very particular advantage of the present invention employing amicroreactor, or a continuous flow reactor with the before said lateraldimensions, the number of separating steps can be reduced andsimplified, and may be devoid of time and energy consuming, e.g.intermediate, distillation steps. Especially, it is a particularadvantage of the present invention employing a microreactor, or acontinuous flow reactor with the before said lateral dimensions, thatfor separating simply phase separation methods can be employed, and thenon-consumed reaction components may be recycled into the process, orotherwise be used as a product itself, as applicable or desired.

In addition to the preferred embodiments of the present invention usinga microreactor according to the invention, in addition or alternativelyto using a microreactor, it is also possible to employ a plug flowreactor or a tubular flow reactor, respectively.

Plug flow reactor or tubular flow reactor, respectively, and theiroperation conditions, are well known to those skilled in the field.

Although the use of a continuous flow reactor with upper lateraldimensions of about ≤5 mm, or of about ≤4 mm, respectively, and inparticular of a microreactor, is particularly preferred in the presentinvention, depending on the circumstances, it could be imagined thatsomebody dispenses with an microreactor, then of course with yieldlosses and higher residence time, higher temperature, and instead takesa plug flow reactor or turbulent flow reactor, respectively. However,this could have a potential advantage, taking note of the mentionedpossibly disadvantageous yield losses, namely the advantage that theprobability of possible blockages (tar particle formation by non-idealdriving style) could be reduced because the diameters of the tubes orchannels of a plug flow reactor are greater than those of amicroreactor.

The possibly allegeable disadvantage of this variant using a plug flowreactor or a tubular flow reactor, however, may also be seen only assubjective point of view, but on the other hand under certain processconstraints in a region or at a production facility may still beappropriate, and loss of yields be considered of less importance or evenbeing acceptable in view of other advantages or avoidance ofconstraints.

In the following, the invention is more particularly described in thecontext of using a microreactor. Preferentially, a microreactor usedaccording to the invention is a ceramic continuous flow reactor, morepreferably a SiC (silicon carbide) continuous flow reactor, and can beused for material production at a multi-to scale. Within integrated heatexchangers and SiC materials of construction, it gives optimal controlof challenging flow chemistry application. The compact, modularconstruction of the flow production reactor enables, advantageously for:long term flexibility towards different process types; access to a rangeof production volumes (5 to 4001/h); intensified chemical productionwhere space is limited; unrivalled chemical compatibility and thermalcontrol.

Ceramic (SiC) microreactors, are e.g. advantageously diffusion bonded 3MSiC reactors, especially braze and metal free, provide for excellentheat and mass transfer, superior chemical compatibility, of FDAcertified materials of construction, or of other drug regulatoryauthority (e.g. EMA) certified materials of construction. Siliconcarbide (SiC), also known as carborundum, is a containing silicon andcarbon, and is well known to those skilled in the art. For example,synthetic SiC powder is been mass-produced and processed for manytechnical applications.

For example, in the embodiments of the invention the objects areachieved by a method in which at least one reaction step takes place ina microreactor. Particularly, in preferred embodiments of the inventionthe objects are achieved by a method in which at least one reaction steptakes place in a microreactor that is comprising or is made of SiC(“SiC-microreactor”), or in a microreactor that is comprising or is madeof an alloy, e.g. such as Hastelloy C, as it is each defined hereinafter in more detail.

Thus, without being limited to, for example, in an embodiment of theinvention the microreactor suitable for, preferably for industrial,production an “SiC-microreactor” that is comprising or is made of SiC(silicon carbide; e.g. SiC as offered by Dow Corning as Type G1SiC or byChemtrix MR555 Plantrix), e.g. providing a production capacity of fromabout 5 up to about 400 kg per hour; or without being limited to, forexample, in another embodiment of the invention the microreactorsuitable for industrial production is comprising or is made of HastelloyC, as offered by Ehrfeld. Such microreactors are particularly suitablefor the, preferably industrial, production of fluorinated productsaccording to the invention.

In order to meet both the mechanical and chemical demands placed onproduction scale flow reactors, Plantrixmodules are fabricated from3M™SiC (Grade C). Produced using the patented 3M (EP 1 637 271 B1 andforeign patents) diffusion bonding technology, the resulting monolithicreactors are hermetically sealed and are free from welding lines/jointsand brazing agents. More technical information on the Chemtrix MR555Plantrix can be found in the brochure “CHEMTRIX—Scalable FlowChemistry—Technical Information Plantrix® MR555 Series, published byChemtrix BV in 2017, which technical information is incorporated hereinby reference in its entirety.

Apart from the before said example, in other embodiments of theinvention, in general SiC from other manufactures, and as known to theskilled person, of course can be employed in the present invention.

Accordingly, in the present invention as microreactor also the Protrix®of by Chemtrix can be used. Protrix® is a modular, continuous flowreactor fabricated from 3M® silicon carbide, offering superior chemicalresistance and heat transfer. In order to meet both the mechanical andchemical demands placed on flow reactors, Protrix® modules arefabricated from 3M® SiC (Grade C). Produced using the patented 3M (EP 1637 271 B1 and foreign patents) diffusion bonding technology, theresulting monolithic reactors are hermetically sealed and are free fromwelding lines/joints and brazing agents. This fabrication technique is aproduction method that gives solid SiC reactors (thermal expansioncoefficient=4.1×10⁻⁶K⁻¹).

Designed for flow rates ranging from 0.2 to 20 ml/min and pressures upto 25 bar, Protrix® allows the user to develop continuous flow processesat the lab-scale, later transitioning to Plantrix® MR555 (×340 scalefactor) for material production. The Protrix® reactor is a unique flowreactor with the following advantages: diffusion bonded 3M® SiC moduleswith integrated heat exchangers that offer unrivaled thermal control andsuperior chemical resistance; safe employment of extreme reactionconditions on a g scale in a standard fumehood; efficient, flexibleproduction in terms of number of reagent inputs, capacity or reactiontime. The general specifications for the Protrix® flow reactors aresummarized as follows; possible reaction types are, e.g. A+B→P1+Q (or C)P, wherein the terms “A”, “B” and “C” represent educts, “P” and “P1”products, and “Q” quencher; throughput (ml/min) of from about 0.2 up toabout 20; channel dimensions (mm) of 1×1 (pre-heat and mixer zone),1.4×1.4 (residence channel); reagent feeds of 1 to 3; module dimensions(width×height) (mm) of 110×260; frame dimensions (width×height×length)(mm) approximately 400×300×250; number of modules/frame is one (minimum)up to four (max.). More technical information on the ChemtrixProtrix®reactor can be found in the brochure “CHEMTRIX—Scalable FlowChemistry—Technical Information Protrix®, published by Chemtrix BV in2017, which technical information is incorporated herein by reference inits entirety.

The Dow Corning as Type GlSiC microreactor, which is scalable forindustrial production, and as well suitable for process development andsmall production can be characterized in terms of dimensions as follows:typical reactor size (length×width×height) of 88 cm×38 cm×72 cm; typicalfluidic module size of 188 mm×162 mm. The features of the Dow Corning asType GlSiC microreactor can be summarized as follows: outstanding mixingand heat exchange: patented HEART design; small internal volume; highresidence time; highly flexible and multipurpose; high chemicaldurability which makes it suitable for high pH compounds and especiallyhydrofluoric acid; hybrid glass/SiC solution for construction material;seamless scale-up with other advanced-flow reactors. Typicalspecifications of the Dow Corning as Type GlSiC microreactor are asfollows: flow rate of from about 30 ml/min up to about 200 ml/min;operating temperature in the range of from about −60° C. up to about200° C., operating pressure up to about 18 barg (“barg” is a unit ofgauge pressure, i.e. pressure in bars above ambient or atmosphericpressure); materials used are silicon carbide, PFA (perfluoroalkoxyalkanes), perfluoroelastomer; fluidic module of 10 ml internal volume;options: regulatory authority certifications, e.g. FDA or EMA,respectively. The reactor configuration of Dow Corning as Type GlSiCmicroreactor is characterized as multipurpose and configuration can becustomized. Injection points may be added anywhere on the said reactor.

Hastelloy® C is an alloy represented by the formula NiCr21Mo14W,alternatively also known as “alloy 22” or “Hastelloy® C-22. The saidalloy is well known as a highly corrosion resistantnickel-chromium-molybdenum-tungsten alloy and has excellent resistanceto oxidizing reducing and mixed acids. The said alloy is used in fluegas desulphurization plants, in the chemical industry, environmentalprotection systems, waste incineration plants, sewage plants. Apart fromthe before said example, in other embodiments of the invention, ingeneral nickel-chromium-molybdenum-tungsten alloy from othermanufactures, and as known to the skilled person, of course can beemployed in the present invention. A typical chemical composition (allin weight-%) of such nickel-chromium-molybdenum-tungsten alloy is, eachpercentage based on the total alloy composition as 100%: Ni (nickel) asthe main component (balance) of at least about 51.0%, e.g. in a range offrom about 51.0% to about 63.0%; Cr (chromium) in a range of from about20.0 to about 22.5%, Mo (molybdenum) in a range of from about 12.5 toabout 14.5%, W (tungsten or wolfram, respectively) in a range of fromabout 2.5 to about 3.5%; and Fe (iron) in an amount of up to about 6.0%,e.g. in a range of from about 1.0% to about 6.0%, preferably in a rangeof from about 1.5% to about 6.0%, more preferably in a range of fromabout 2.0% to about 6.0%. Optionally, the percentage based on the totalalloy composition as 100%, Co (cobalt) can be present in the alloy in anamount of up to about 2.5%, e.g. in a range of from about 0.1% to about2.5%. Optionally, the percentage based on the total alloy composition as100%, V (vanadium) can be present in the alloy in an amount of up toabout 0.35%, e.g. in a range of from about 0.1% to about 0,35%. Also,the percentage based on the total alloy composition as 100%, optionallylow amounts (i.e. ≤0.1%) of other element traces, e.g. independently ofC (carbon), Si (silicon), Mn (manganese), P (phosphor), and/or S(sulfur). In such case of low amounts (i.e. ≤0.1%) of other elements,the said elements e.g. of C (carbon), Si (silicon), Mn (manganese), P(phosphor), and/or S (sulfur), the percentage based on the total alloycomposition as 100%, each independently can be present in an amount ofup to about 0.1%, e.g. each independently in a range of from about 0.01to about 0.1%, preferably each independently in an amount of up to about0.08%, e.g. each independently in a range of from about 0.01 to about0.08%. For example, said elements e.g. of C (carbon), Si (silicon), Mn(manganese), P (phosphor), and/or S (sulfur), the percentage based onthe total alloy composition as 100%, each independently can be presentin an amount of, each value as an about value: C≤0.01%, Si≤0.08%,Mn≤0.05%, P≤0.015%, S≤0.02%. Normally, no traceable amounts of any ofthe following elements are found in the alloy compositions indicatedabove: Nb (niobium), Ti (titanium), Al (aluminum), Cu (copper), N(nitrogen), and Ce (cerium).

Hastelloy® C-276 alloy was the first wrought, nickel-chromium-molybdenummaterial to alleviate concerns over welding (by virtue of extremely lowcarbon and silicon contents). As such, it was widely accepted in thechemical process and associated industries, and now has a 50-year-oldtrack record of proven performance in a vast number of corrosivechemicals. Like other nickel alloys, it is ductile, easy to form andweld, and possesses exceptional resistance to stress corrosion crackingin chloride-bearing solutions (a form of degradation to which theaustenitic stainless steels are prone). With its high chromium andmolybdenum contents, it is able to withstand both oxidizing andnon-oxidizing acids, and exhibits outstanding resistance to pitting andcrevice attack in the presence of chlorides and other halides. Thenominal composition in weight-% is, based on the total composition as100%: Ni (nickel) 57% (balance); Co (cobalt) 2.5% (max.); Cr (chromium)16%; Mo (molybdenum) 16%; Fe (iron) 5%; W (tungsten or wolfram,respectively) 4%; further components in lower amounts can be Mn(manganese) up to 1% (max.); V (vanadium) up to 0.35% (max.); Si(silicon) up to 0.08% (max.); C (carbon) 0.01 (max.); Cu (copper) up to0.5% (max.).

In another embodiments of the invention, without being limited to, forexample, the microreactor suitable for the said production, preferablyfor the said industrial production, is an SiC-microreactor that iscomprising or is made only of SiC as the construction material (siliconcarbide; e.g. SiC as offered by Dow Corning as Type G1 SiC or byChemtrix MR555 Plantrix), e.g. providing a production capacity of fromabout 5 up to about 400 kg per hour.

It is of course possible according to the invention to use one or moremicroreactors, preferably one or more SiC-microreactors, in theproduction, preferably in the industrial production, of the fluorinatedproducts according to the invention. If more than one microreactor,preferably more than one SiC-microreactors, are used in the production,preferably in the industrial production, of the fluorinated productsaccording to the invention, then these microreactors, preferably theseSiC-microreactors, can be used in parallel and/or subsequentarrangements. For example, two, three, four, or more microreactors,preferably two, three, four, or more SiC-microreactors, can be used inparallel and/or subsequent arrangements.

For laboratory search, e.g. on applicable reaction and/or upscalingconditions, without being limited to, for example, as a microreactor thereactor type Plantrix of the company Chemtrix is suitable. Sometimes, ifgaskets of a microreactor are made out of other material than HDPTFE,leakage might occur quite soon after short time of operation because ofsome swelling, so HDPTFE gaskets secure long operating time ofmicroreactor and involved other equipment parts like settler anddistillation columns.

For example, an industrial flow reactor (“IFR”, e.g. Plantrix® MR555)comprises of SiC modules (e.g. 3M® SiC) housed within a (non-wetted)stainless steel frame, through which connection of feed lines andservice media are made using standard Swagelok fittings. The processfluids are heated or cooled within the modules using integrated heatexchangers, when used in conjunction with a service medium (thermalfluid or steam), and reacted in zig-zag or double zig-zag, meso-channelstructures that are designed to give plug flow and have a high heatexchange capacity. A basic IFR (e.g. Plantrix® MR555) system comprisesof one SiC module (e.g. 3M® SiC), a mixer (“MRX”) that affords access toA+B P type reactions. Increasing the number of modules leads toincreased reaction times and/or system productivity. The addition of aquench Q/C module extends reaction types to A+B P1+Q (or C) P and ablanking plate gives two temperature zones. Herein the terms “A”, “B”and “C” represent educts, “P” and “P1” products, and “Q” quencher.

Typical dimensions of an industrial flow reactor (“IFR”, e.g. Plantrix®MR555) are, for example: channel dimensions in (mm) of 4×4 (“MRX”,mixer) and 5×5 (MRH-I/MRH-II; “MRH” denotes residence module); moduledimensions (width×height) of 200 mm×555 mm; frame dimensions(width×height) of 322 mm×811 mm. A typical throughput of an industrialflow reactor (“IFR”, e.g. Plantrix® MR555) is, for example, in the rangeof from about 50 1/h to about 400 1/h. In addition, depending on fluidproperties and process conditions used, the throughput of an industrialflow reactor (“IFR”, e.g. Plantrix® MR555), for example, can alsobe >400 1/h. The residence modules can be placed in series in order todeliver the required reaction volume or productivity. The number ofmodules that can be placed in series depends on the fluid properties andtargeted flow rate.

Typical operating or process conditions of an industrial flow reactor(“IFR”, e.g. Plantrix® MR555) are, for example: temperature range offrom about −30° C. to about 200° C.; temperature difference(service-process)<70° C.; reagent feeds of 1 to 3; maximum operatingpressure (service fluid) of about 5 bar at a temperature of about 200°C.; maximum operating pressure (process fluid) of about 25 bar at atemperature of about ≤200° C.

The following examples are intended to further illustrate the inventionwithout limiting its scope.

EXAMPLES

Following compounds or intermediates are prepared according to thisinvention:

Example 1: Continuous Synthesis of 1233xf Out of HCFC-123 at 800° C. ina Monel-Tube Reactor in Gas Phase

A Monel tube (d=10 cm, volume around 6.5 1, electrically heated, N2-flowduring heating up) was filled with 1 cm Ni-fillings from company Raschig(Germany). Once the reactor temperature reached 800° C., the 123 feedcontrolled with a Bronkhorst flow meter over a vaporizer (operated at100° C.) was adjusted to 600 g/h (3.92 mol) and another Bronkhorst flowmeter at 202 g/h (4.0 mol) chloromethane out of a gas cylinder into theMonel tube. The pressure was kept by a pressure valve at 2 bar abs. Thegas stream leaving the reactor tube was fed over a 1 m cooled pipe (+20°C.) of 1 cm diameter into a water scrubber (operated at roomtemperature) to absorb HCl and to hydrolyze little amounts of phosgenelike side products. A GC/GC-MS analysis of the gas steam leaving thescrubber indicated a quantitative conversion of 123 and selectivity to1233xf of 96%. The gas steam after the scrubber was condensed into astainless steel cylinder (fed inlet over a deep with deep) cooled to−78° C. with CO₂/EtOH.

Example 2: Continuous Synthesis of 1233xf Out of HCFC-123 at 800° C. ina Quartz Glass Tube Reactor in Gas Phase

A quartz tube (d=10 cm, length 30 cm) with electrical heating and aN2-flow during heating up) was filled with 1 cm quartz glass fillings.Once the reactor temperature reached 800° C., the 123 feed controlledwith a Bronkhorst flow meter over a vaporizer (operated at 100° C.) wasadjusted to 200 g/h (1.31 mol) and another Bronkhorst flow meter at 75.7g (1.5 mol mol/h) Chloromethane out of a gas cylinder. The pressure waskept by a pressure valve at 1.2 bar abs. The gas stream leaving thereactor tube was fed over a 1 m cooled pipe (+25° C.) of 1 cm diameterinto a water scrubber to absorb HCl and to hydrolyze potential phosgenelike side products and some unstable intermediates and phosgenes. AGC/GC-MS analysis of the gas steam leaving the scrubber indicated a 81%conversion of 123 and selectivity to 1233xf of 89%. The gas stream afterthe scrubber was condensed into a stainless steel cylinder (fed inletover a deep with deep) cooled to −78° C. with CO₂/EtOH.

Example 3: Synthesis of 1233xf in Liquid Phase Under Phase TransferCatalysis

In a 250 ml Roth autoclave with deep pipe and gas outlet, 50 ml 123 (73g, 0.48 mol) were mixed with 28 g KOH pellets from Aldrich and 30 mldeionized water together with 2 g TBAB (tetrabutylammoniumbomide, 0.006mol) also from Aldrich and the autoclave was closed. The autoclave washeated to 80° C. Afterwards, 73 g (0.48 mol) liquid 123 (using a pistonpump) and 30.29 g (0.6 mol) Chloromethane (over a Bronkhorst flow meterout of a gas cylinder) were fed together over the deep pipe into theautoclave and the pressure was kept at 4 bar abs. with a pressure valveinstalled at the gas outlet of the autoclave. The gas stream leaving thereactor tube was fed over a 1 m cooled pipe (+25° C.) of 1 cm diameterinto a water scrubber to absorb still some present HCl (most of the HClremained in the autoclave). A GC/GC-MS analysis of the gas steam leavingthe scrubber contained no 123 but mainly 1233xf. The gas stream afterthe scrubber was again condensed into a stainless steel cylinder (fedinlet over a deep pipe) cooled to −78° C. with CO₂/EtOH.

Example 4: Fluorination of 1233xf in Liquid Phase to 1234yf

In a 250 ml Roth autoclave with PTFE inliner, a deep pipe and gas exit,30 g (0.23 mol) 1233xf were dissolved in 50 ml anhydrous HF fed out of aHF cylinder. Then SbF₅ (freshly prepared out of SbCl₅ (traces of Cl arenot exchanged so the catalyst is SbCl_(x)F_(5-x), preparation in anotherautoclave) were added. The autoclave with all the raw materials and theSb was heated for 1 h to 95° C. (pressure raised to 10 bar) and wasslowly worked up after cooling down into ice water in a plastic washingbottle with deep pipe. The gas leaving the washing bottle was trappedinto a stainless steel cylinder cooled to −78° C. and consisted out of1234yf with traces of impurities only. Some unconverted 1233xf was foundas 2nd phase in the washing bottle. The isolated yield for 1234yf was76%, the 1233xf found back in the washing bottle indicated a conversionof 79% and a selectivity to 1234yf of 98%.

Example 5: Continuous Preparation of 1234yf Out of 123 in a TwoMicroreactor Reaction Sequence

1st step:

A first 30 ml microreactor made out of Nickel from company Innosyn BV(Geelen, Netherlands) for Carbene generation (heated to 700° C.,pressure kept at 12 bar abs. by a pressure valve) and a 2nd 27 mlmicroreactor made out of SiC from Chemtrix were installed and operatedin row. In a 1st step, HFC 243db is formed by CF₃—CC12:—Carbeneinsertion (formed out of 123 which was fed as liquid into microreactor)into Chloromethane. In comparison to the simple tube reactor out ofNickel or quartz glass, the residence time in this microreactor iscarefully adjusted so as Zero 1233xf is formed and quantitative 123conversion is achieved. After cooling the gas stream leavingmicroreactor 1 to 0° C. over a 100 cm coil (diameter 1 cm) made out ofHastelloy C4, most of the formed HCl from 1st stage is stripped over aCyclone and liquid 243db is collected.

2nd step:

Crude HCFC 243db is not further purified and fed together as HF/Sb molar20:1 mixture (Sb^(V)) into the 2nd microreactor heated to 98° C.,pressure kept at 11 bar abs.

See FIG. 1 for the synthesis of compound 1234yf out of compound 123.

In microreactor 2, chlorine/fluorine exchange happened in situ followedby HCl-elimination catalyzed by the Lewis acid function of theSb-catalyst. Another (not drawn) coil cooler operated at 0° C. andanother cyclone was applied after microreactor 2 to strip HCl. After thecyclone, the process stream entered a phase separator cooled to −10° C.where a crude 1234yf gives the lower phase which was subjected to acontinuous fine distillation. In a stainless steel column pure 1234yf ata transition temperature of +35° C./10 bar abs. The upper phase of theseparator is fed back into the HF/catalyst storage tank, 5 mol-% (vs.Sb-concentration) of F₂ is added (Cl₂ also would be possible) into thestream to convert some formed low reactive Sb^(III) back to the Sb^(V)oxidation state (some deactivation of Sb^(V)→Sb^(III) happens duringfluorination).

In this procedure, 300 g (3.27 mol) 123 per hour and 166.6 g (3.3 mol)Chloromethane per hour were reacted after 2 steps in 92% yield and full123 conversion to 1234yf. In seldom case of some traces of hydrolysablefluoride in the final distilled product, a further purification over NaFpellets was applied.

Example 6: Synthesis of 1234yf Out of 125 in Microreactor

The installation is the same as in example 5 but only the 1^(st)microreactor made out of Nickel is used.

See FIG. 2 for the synthesis of compound 1234yf out of compound 125.

The 360.1 g (3.0 mol) 125 per hour and 161.6 g (3.2 mol) CH₃C1 per houris fed over Bronkhorst flow meters and out of stainless steel cylinderseach into the microreactor kept at 12 bar abs. by a pressure valve.After the microreactor and the coil cooler (1 m length, d=1 cm) operatedat 0° C., some HF with most of the formed HCl is leaving over theCyclone. The product stream after the cyclone is all collected in acooling trap kept at −78° C. An analysis of the gas phase of a carefullyhydrolyzed sample out of that cylinder showed a 75% conversion of 125and selectivity to 1234yf of 98%. The stainless steel column asdescribed in example 5 was used for a fine distillation (at 10 bar abs.)of material previously washed over ice water before distillation. Theachieved 1234yf purity at a transition temperature of 35° C. was 99.9%(GC).

Example 7: Synthesis of 1234yf Out of 243db in Gas Phase with Zn DopedCr₂O₃-Catalyst Over Two Reaction Zones

Apparatus: The 2 zone tube reactor system consists out of 2×25 cmMonel-tube (diameter 5 cm). The 1^(st) zone was filled with Zn dopedCr₂O₃ catalyst pellets. A HF feeding system is installed over avaporizer and consists out of a stainless steel cylinder pressurizedwith N2 (dosage from liquid phase over a Bronkhorst flow meter into thevaporizer). The vaporizer is operated at 120° C. (needed for the 243dbb.p. 77° C.). The zones are separated by a cyclone where almost all HCltogether with most of the HF is stripped out before the material entersthe 2nd zone. The 2nd zone (25 cm) is filled with AlF₃ pellets (d=2 mm)prepared out of commercial AlF₃ powder by pressing. The Pt zone iselectrically heated to 150° C., the 2nd zone to 350° C.

Recipe for the preparation of the catalysts:

Zn-doped Cr₂O₃ catalyst preparation: 1 kg (19.2 mol) of Chromia in formof granules of size 0.5-1.4 mm and surface of 50 m²/g (Strem chemicals)was added to a solution of 78.6 g (0.5769 mol) ZnCl₂ in 11 distilledwater and stirred for 1 h at room temperature. Afterwards, the materialwas dried in vacuum (20 mbar/60° C.) until no weight loss could beobserved resulting in particles of size 0.5-1.4 mm with 3 wt.-% Zn. Thiscatalyst was filled into the Pt zone of the reactor and pre-fluorinated2 h with an anhydrous HF stream until no water could be detected anymore in the stream leaving the reactor. The AlF₃-pellets were just driedin N2-stream at 350° C. before usage.

250 g (1.50 mol) 243db per hour was fed together with 150 g (7.5 mol)anhydrous HF per hour over the vaporizer into zone 1 and after havingpassed a cyclone into zone 2. The pressure was kept at 10 bar by apressure valve after reactor 2, another valve at the exit of the cyclone(operated at 21° C.) was adjusted to a material flow of 3 1/minute intoa scrubber system. The gas stream leaving reactor 2 was fed over anothercyclone to strip HCl before it was collected into a cooling trap (−78°C.). All material collected in the cooling trap was carefully washedwith ice water (washing bottle), the gas steam leaving the washingbottle indicated already a 1234yf crude material composition of 98%besides some undefined % impurities. Isolated 1234yf was 78% d. Th. overthe 2 steps.

What is claimed is:
 1. A process for a manufacture of a compound 1233xf(2-chloro-1,1,1-trifluoropropene) comprising the steps of: (a) providinga compound HCFC 123 (2,2-dichloro-1,1,1-trifluoroethane) as a startingmaterial; (b) generating a carbene (CF₃—C(:)Cl) out of the compound HCFC123 (2,2-dichloro-1,1,1-trifluoroethane) provided under (a), wherein (i)the carbene generation is performed in a liquid phase with a phasetransfer catalyst and a base; or (ii) the carbene generation isperformed in gas phase (vapor-phase) by high temperature thermolysis;(c) mixing and reacting the carbene (CF₃—C(:)Cl) formed in (b) withmethyl chloride (CH₃C1) and elimination of HCl (hydrogen chloride), andfurther dehydrochlorination (—HCl); (d) withdrawing the reaction mixtureobtained in (c) from the said reactor in (c) to yield a 1233xf(2-chloro-1,1,1-trifluoropropene) comprising product, preferably a1233xf (2-chloro-1,1,1-trifluoropropene) product; (e) optionallywithdrawing the HCl formed in the reactor in (c) as an effluent fromreaction mixture obtained in (d); and (f) optionally purifying and/orisolating the 1233xf (2-chloro-1,1,1-trifluoroprop ene) product obtainedin (d), or optionally in (e), to yield purified and/or isolated 1233xf(2-chloro-1,1,1-trifluoropropene).
 2. The process according to claim 1,wherein the high temperature thermolysis in step (b)-(ii) denotes athermal decomposition performed at a temperature of about at least 400°C.; preferably wherein the high temperature thermolysisis performed at atemperature in the range of about 400° C. to about 950° C.; morepreferably, the high temperature thermolysis is performed at atemperature in the range of about 500° C. to about 900° C.; still morepreferably, the high temperature thermolysis is performed at atemperature in the range of about 700° C. to about 800° C.
 3. Theprocess according to claim 1, wherein the phase transfer catalyst instep (b)-(i) comprises or consists of a compound of at least one of thecompound classes of a) linear or cyclic ammonium salts, b) heterocyclicammonium salts, c) non-ionic phase transfer compounds, d) phosphoniumsalts, and combinations thereof.
 4. The process according to claim 1,wherein the base in step (b)-(i) comprises or consists of (i) aninorganic substance selected from the group consisting of KOH, NaOH,LiOH, Ca(OH)₂, or combinations thereof, or comprises or consists of (ii)a metal organic substance selected from the group consisting ofLi-organyl compounds, alkali metals like Na and K, or combinationsthereof.
 5. The process according to claim 1, wherein at least onereaction step, as defined in any of the steps (b)-(i) to (b)-(ii), inthe said reactors is performed in a continuous flow reactor; optionallywherein (i) the continuous flow reactor is a pipe-like continuous flowreactor, preferentially with minimal lateral dimensions of about >5 mm,more preferentially a pipe-like continuous flow reactor in coiled form(tube-like coiled reactor), or (ii) the continuous flow reactor is amicroreactor, preferably with upper lateral dimensions of up to about <5mm.
 6. The process according to claim 5, wherein the at least onereaction step in the said reactors is performed (i) in a continuous flowreactor that is a coiled continuous flow reactor; optionally wherein (i)the coiled continuous flow reactor is a coiled pipe-like continuous flowreactor, preferentially with minimal lateral dimensions of about >5 mm.7. The process according to claim 5, wherein the at least one reactionstep in the said reactors is performed (ii) in a continuous flow reactorthat is a microreactor, preferably with upper lateral dimensions of upto about ≤5 mm.
 8. The process according to claim 7, wherein the atleast one reaction step is performed (ii) in a microreactor under one ormore of the following conditions: flow rate: of from about 10 ml/h up toabout 4001/h; temperature: of from about 30° C. up to about 150° C.;pressure: of from about 5 bar up to about 50 bar; residence time: offrom about 1 minute up to about 60 minutes.
 9. The process according toclaim 5, wherein at least one of the said continuous flow reactors, is aSiC-continuous flow reactor.
 10. The process according to claim 5,wherein at least one of the microreactors is a SiC-microreactor.